HU228186B1 - Concept for slurry separation and biogas production - Google Patents

Description

The process of the present invention comprises (i) collecting organic material containing solid and / or liquid parts and (ii) carrying out the following steps on the organic material: (a) hydrolyzing the organic material by high pressure lime at 100 ° C to 220 ° C; wherein the lime is calcium hydroxide and / or calcium oxide; and (b) the ammonia is extracted from the organic material treated with high pressure lime, wherein the lime added to recover the ammonia and disinfect the organic material precipitates the dissolved orthophosphates. Subsequently, (iii) a processed organic material is produced which contains a reduced amount of viable microbial organism and / or prion. Finally (in a sheet), the processed organic material is fed to a biogas-producing digester, in which the processed organic material is digested and thus biogas is produced.

The biogas plant produces biogas by anaerobic fermentation of processed organic material containing solid and liquid components. The plant comprises at least the following units: (i) an extraction tank (12) for removing ammonia from the organic material treated in the high-pressure lime digestion unit (9), wherein the extraction tank (12) is connected to an absorption unit for absorbing and condensing the recovered ammonia; ii) digestion tank (13, 14, 15) for anaerobic digestion of treated and ammonium depleted organic matter in the high pressure lime digestion unit (9) resulting in biogas production and (iii) high pressure lime digestion unit (9) for hydrolysis of the organic material. The high pressure lime cooking unit (9) and the extraction tank (12) are connected such that organic material treated with the high pressure lime cooking unit (9) can be discharged from the high pressure lime cooking unit (9) to the extraction tank (12) and 12) and the biogas generating digestion tank (13, 14, 15) are connected such that the high pressure lime treated and ammonia-free organic material is fed from the extraction tank (12) to the biogas generating digestion tank (13, 14, 15) and wherein the high pressure lime digester (13). 9) and the extraction vessel (12) are further connected to each other in such a way that the recovered ammonia can be transported from the high-pressure lime cooking unit (9) to the extraction vessel (12) and absorbed in an ammonia absorption unit (21).

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Methods for Viable Microorganisms in Organic Materials and / or

PRYOMS FOR REDUCING NUMBERS AND THE PROCEDURE FOR IMPLEMENTING THE PROCEDURE

The present invention relates, on the one hand, to anaerobic digestion of organic fertilizers, compost and the like. The process according to the invention is suitable for refining the nutrients in digested biomass into commercial grade fertilizers. According to the invention, the biogas and slurry separation system can advantageously be integrated with a backyard farm into a general system in which the home and farm are optimally utilized.

A further aspect of the invention is the potential applications for the disposal of animal waste in the form of animal residues, slaughterhouse waste, meat and bone meal, etc. Such waste is refined at the plant into fertilizers suitable for fertilising agricultural land. Throughout the process, the amount of BSE prions or other jokes that may be present is significantly reduced and completely destroyed. The animal product is utilized in the system of the invention not as feed but as fertilizer. By eliminating BS £ phones that may be present in on-farm biomass and by using refined biomass as a fertilizer instead of feed, the risk of infecting animals or humans with BSE-pnons or their variants is significantly reduced.

The internal options are, on the one hand, quality aspects related to the management of the animal habitat, including industrial hygiene, animal care, control of gas and dust emissions, and feed safety. The external options mainly include energy production and control of the release of nutrients and greenhouse gases into the environment, the sale of good quality feed products and an alternative way of removing animal residues and other similar materials.

Ammonia chemists are well known in the art and the recovery of ammonia from various liquids is a well-known industrial process,

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2 were reported by candy makers (see Criminal El. Al. 1-995; Chacuk et al. 1994; Paralytic and Cubero 1996) and by urban authorities in the treatment of infertility to fill areas (Gheung et al. 1997). Ammonia can be extracted from pig manure in the same way as in industry (Liao et al. 1995./

The principle of large-scale production of ammonia is to raise the pH and to aerate and heat the wastewater or sludge. Often, Ca (ÖH} ₂ or CaQ is used to increase the ρ. Value. However, other bases can also be used, such as MaGM or KOK. However, calcium oxide <

used in the cement industry so that it can be obtained at cheap and bulk prices.

Where the recovered ammonia is absorbed and ammonia machine concentrate is produced, sulfuric acid is often used in the absorption column. Sulfuric acid is also an industrial bulk product and is available in a technical grade which makes it suitable for use in absorption columns used to recover ammonia from slurry and other wastewater (see Sacuk et al. 1994),

Experience with sugar production has shown that the most suitable parameter values are: 70 ° C; a pH of about 10-12; 1: 800 liquid to gas ratio; and 96% efficiency,

When ammonia is recovered from the slurry, it has been found that the optimum parameter values at low temperatures are: 22 ° C; a pH of about 10-12; 1: 2000 liquid to gas ratio: 90% efficiency; and 150 hours of operation (Liao et al. 1995).

Below are some documents that provide some of the above knowledge:

Paralytic G. G, and Cubero Μ. T. G, (1996) Ammonia elimination from bee! Radial faetory condensate streams by a stripping-reabsorbing system. Zuckerindustrie 121, 721-726,

For sin.U., Buczys Ft, Bruhns M., and Buchhoiz K, (1998) Ammonia sthpping. Zeckenndusfrte 120,960-969.

Chacuk A ,,. Zarzyckl R., and Leiek J. (1994) A mathematical model for the absorption of ammonia from condensates. Zuckerindustrie 119, 1008-1015.

Cheung K. C. Chu L M., and Wong Μ. H. (1997) Ammonia strippsng as a pretreatment forearl leachate. Water Air and Sóit Poilullon 94,209-221.

Liao, Ρ. H., Cben A., and Lo Κ. V. (1995) Removal of Nitrogen from Swine Menu «* * * <« ♦ ♦ Wasfewaters by-ammonia slrtpping. Biotechnology & Applied Mlcrobtology 54.1720.

Prior to anaerobic digestion, heat pre-treatment of biomass is a well-known technology (see Li and Women, 1992). In recent years, Cambí AS (Biliingstad, Norway) has used large-scale pre-treatment of urban waste heat,

Wang el al. (1997a and b) found that pre-treatment of urban waste with SCYC temperature and hydraulic reflux for 8 days resulted in a higher formation of 52J% methane than before. A similar result was obtained by Tanaka et al (1997), who combined this solution with alkaline bydroilysis, and thus achieved an extremely high 209% increase in gas production. Me-Carty et al. Have done a number of studies showing that heat treatment combined with alkaline hydrolysis significantly increases gas formation. However, the pH should be maintained at about 19 to about 12, preferably 11 or higher, before chemical hydrolysis results in significant excess gas formation.

Wang el al. (1997) show that starting values for ammonia recovery as described in Section 2.1 (about 10-12, preferably 11 or higher pH and about 79 ° C or higher for one week) increase the amount of gas produced.

Below are some documents that provide some of the above information:

Li Y. Y ,, and Women 7. (1992) Upgradation of anaerobic digestion of waste activated slurry bv tbermal pre-irealment, Water Science and Technology 26,3-4.

McCarty P. L. Y'oung L, Y. Gossett J. M., Stuckey D. C., and Healy Jr. J. B. Heat trealmenf for increasing organic materfals. Stanford Universify, Caísfornia 94305, USA,

Tanaka S., Kobayashl T. Kamiyama K. and Bíldan M. L. N. S. (1997) Effects of thermo-chemical pre-treatment on anaerobic digestion of waste activated sludge, Water Science and Technology 35,209-215.

Wang Q., Noguchi G., Hara Y., Sharon C., Kakimoto K., and Kató Y. (1997a) Studies on anaerobic digestion mechanisms: influence of pre-treatment temperature on waste activated sludge. Environmentsi Technology 18,999-1008.

Wang Q., Noguchi C, Kg Kunínobu M, Hara Y ,, Kakimoto K. Ogawa Η. I. And Kató Y. (1997b) Influence of hydrautic retention time on anaerobic digestion of pre-treafed ♦ X

.... 4 ski resorts. Biotechnology Tecnnlques 11,105-198,

The removal of slurry and its spreading to the ground prior to disinfection of the slurry is an extremely important task in preventing the spread of animal viruses, bacteria and parasites (see Bendixen 1999). Anaerobic digestion has been shown to be effective in reducing the number of zoonoses in the slurry, but is not suitable for the complete elimination of these organisms (Bendixen 1999; Pagliía et al. 2000). The use of calcium exide to disinfect wastewater has also shown that Ascarls eggs and parasites (Eriksen et al. 1998) and viruses are significantly reduced but cannot be completely eliminated (Turner and 'Burton 1997).

The following are some of the documents that contain the Knowledge above

Bendixen H. d. Hygiene safety resume of scienfíflc investigatlons In Denmark (sanitation requirements in Danlsh biogas plants). Hohenheímer Semínar IEA Bloenergy Workshop Maron 1999.

Eríksen L, Andreasen P. Soc.

Pagílla K, R., Kim H, & gheunbam T. (2000) Treatment of aerobic thermopile and anaerobic mesoplle by swine waste. Water Research 34,2747-2753.

Turner C, and Burton C, H. (1997) The inactivation of viral In plg slurries; a revlew. Bíoresoorce Technology 81.9-20.

Foam formation associated with anaerobic digestion poses a serious problem for the functioning of roasting tanks. Many antifoaming agents are commercially available which contain various polymers, vegetable oils and various salts (see, for example, Vardar-Sukan 1998). A. Polymers, however, often pose environmental problems and in many cases are expensive while being less effective.

Related literature;

Vardar-Sukan F. (1998) Foamíng; consequences, preventlon and destructlon. Biotechnology Advances 18,913-948.

Calcium ions are well known for flocculating substances and particles due to the formation of calcium bridges between organic and inorganic materials in solution or suspension, which produce flakes from the particles (see Saran and Vesilind 1996). calcium is also used for the drainage of wastewater (see Hlggíns and Novak 1997).

The following are the documents containing the Knowledge relating thereto;

Mlggins M, d. and Novak j. T. (1997), Effects of cat ions on seftling and dewatenng of activated siudge's: Lahoratary results. Water Envlronmenf Research 69, 215-224.

Sanln F, and Veslhnd P. A, (1996) Synthetlc Sludge: Physicat / Chemical Methods in Understanding Bio Flocculation, Water Enviromental Research 58,927-933.

Decanting centrifuges have been used by many industries in the last 100 years: · One of the most recent examples of decanting centrifuges is the Novo Nordlsk plant (Kalundborg), where all the waste from large-scale insulin digesters is treated with such centrifuges. Decanting centrifuges can also be used to drain urban wastewater (see Alfa Lava's A / S). Decanting centrifuges separate the dry (solids) from the slurry or waste, and the aqueous phase or waste water is led to a conventional sewage treatment plant.

The ghosts of separating bovine and livestock manure and degassed slurry first of all showed that the decanalizing centrifuges were able to handle all the solids without difficulty, and they also found that the centrifuges were able to prod 6080% of total phosphorus and only 14% of total nitrogen are removed (see Moher et al. 1999; Moher 2000a). In the case of cattle and pig manure, the corresponding values were slightly lower. It is necessary to note that only 14% of the total nitrogen is removed from the waste material.

The total cost of treatment is 5 QKR per cubic meter of slurry of 26009 tonnes or more. In cases where the amount of slurry exceeds 20000 tonnes, decanting centrifuges can be economically operated and provide a cheap means of dry matter and total amount of phosphorus (see Moher et al. 1999),

Under normal circumstances, it is not worth treating the slurry in a decanter centrifuge as it does not result in either a reduction in quantity or any other benefit to the farmers. After the application of the treated slurry to the production area, the reduction in the amount of ammonia is somewhat mitigated by the "infiltration rate" of ammonia "e" to the soil (see Malter 2000b). However, this is not sufficient reason for farmers to use decanting centrifuges.

Hereinafter, documents containing knowledge of the foregoing will be provided;

Moiter Η. B. (2000a) Opkoncentrering af naeringsstoTíer i husdyrgdning med decantercenírifuge og skruepresse. Note 12, September 2000, Forskníngscenter Bygholm,

Moiler Η. B. (2000b) Gode msultater med at separere gyiie. Maskinbladet August 25, 2000.

Malter Η. B, Lund !, and Sommer 3, G. (1009) Solid-ligand separation of input fluids; efficiency and cost.

Alpha avatars: A / S Gylíeseparerlng. Separeringsresuitater med áeeanterceníhfuge.

The dissolved phosphorus precipitates almost immediately after the addition of calcium (Ca ₃ (PO ₄ ) ₂ ) to the slurry (see Cheung; et al. 1995).

Related literature;

Cheung K. C.>. Chu L M ,, and Wong Μ. H. (109?) Ammonia stripping as a pretreatmenf for landfiii teachafe. Wáter Air and Soll Pollutlon 94,209-221.

Another important consideration is that phosphorus precipitation and ammonia recovery together prevent the formation of struvite (MgNkLPCh}, which is a major operational problem in heat exchangers and slurry transport via slurry (see Kröger 1993) and the removal of phosphorus by the production of CaPO ₄ The removal of phosphorus and ammonia can prevent the formation of struvite.

Kroger (1993) Struvit danneise I biogasf liesaul g. Roger WasteSystems AS.

In the last 10 years, systems have been introduced that provide final treatment and membrane filtration of wastewater. Examples of such plants are BioScan A / S and Ansager A / S. Such plants are also plants whose operation is based on the compression of steam, so be it Funki A / S or Bjssrnkjaer Maskinfabnkker A / S. These systems generally result in gross processing costs of 50-100 DKR per slurry of 1 nr. In addition, these plants are only suitable for processing pig manure, * * X *

The quantity reduction achieved in such plants is generally no more than S8-8%, which means that the use of the remaining part on the land is in any case dependent on conventional means. As a result, these plants are not competitive due to their cost levels and / or limited volume reduction

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However, we consider it important to examine and determine the operating costs of these plants. It is also important to examine the amount of energy used as electricity. The power provided by the mechanical steam compressor is approximately 50 kWh per tonne of treated slurry. This means that the membranes are capable of displacing vapor deposition technologies, assuming that the filtrate contains only a lot of water phases and a minimum amount of solids that do not cause calcification problems,

In the following, we will provide such documents. in which knowledge of the foregoing is found;

Y. (1984) Singie sludge nitrogen removal in an oxydatlon ditch. Water Research 18,1493-1500.

Blouin, M., Nightlife, G., Beudet, R., and Shacue, M. (1988) Aerobic biodegradation of organic malt from swine waste. Bfoiogfoal Wastes 25,127-139.

Boubabiia E, H., Aim R. 8., and Bolsson H. (1993) Micro filtration of an actlvated slurry submerged membrane with Irish bubbling (application to wastewater treatment). Desallnatlon 118,315-322.

Búdon C. H. Sneath R, W., Misselbrook T. H., and Pain 8. F. (1998) Journal of Agrfoaltura! Engineerlng Research 71,203.

Camarro, L., Diaz, J., and Romero, F (1998) Feline treatments for anaerobic digestion of effluents. Biomass and Bfoenergy 11,483-489.

Doyle Y. and de la Neue J. (1987) Aerobic treatment of swine manure:

Physicoohemical aspects. Blological Wastes 22,187-208.

Engelhard, N., Firk, W, and Warnken, W (1996) Integration of membrane filtration information into an actlvated slide process in ammunition wastewater treatment. Water Science and Technology 38,429-438,

Garraway 3. L. (1982) Investigations on aerobic treatment of pig slurry. Agricuiturai Wastes 4,131-142.

Glnnivars, M.J. (1933) The effect of aerosol on odor and soils of pigs Agricuiturai Wastes 7,197-207,

... 8 - Gnenc 1. E, and Hanemo P. (1985) Nitrification in rotating dsc systems-). Crtteria tor iransitton i write oxygen to ammonia rate limit. Water Research 19,11191127.

Beolt J. A ..; Neilson D. J. Uu W., and Boon Ρ, N. (1998) A dual-function membrane bioreactor system for enhanced aerobic remodeling of high-strength industrial waste, Water Science and Technology 38,413-420.

Siiva C.M., Reeve D, W., Húsain H „Rabié H.R., and Woodhouse K.A. (2000)

Journal of Membrane Science 173.87-98,

Visvanathan C. <Yang B-B ,, Pastamere S '., And Maylhanukhraw R. (1997) Application of air back flushing in membrane bioreactor. Water Science and Technology 36-, 259268,

Zaloum R., Coron-Ramstrím A.-F. Gebr, R. (1998) Flnal clarification by integrated filtration of the aotivated siudge aeration. Environmenial Technology 17, 10071014.

Heat treatment and chemical hydrolysis at temperatures below 10 ° C, as well as pressure of about 1 x 10 ^δ Pa due to heb, are only one of many possibilities for the production of biogas from organic material. However, with such treatments, the complex hydrocarbons, i.p. cellulose, hemicelluloses and lignin cannot be completely bidroylated. By such treatment can not be produced from straw, maize and other cereals methane (see Bjerre et al 1998; Schmidt and Thomsen 1998; Thomsen and Sohmidt 1993; Strobl and Rai 1908), at a temperature above 100 ^ö with alkali lime cooking these materials are easily adapted may be used to break down mlcrab (see Curelii et al. 1997; Chang et al. 1997; Chang et al. 1998).

By using this treatment, 0.5 mm cellulose fibers of cane (4% calcium oxide content, 2 ° C ^e C and 1.6 x ^{10 8} Pa) can be comminuted into small amounts of organic acids, formic acid, acetic acid, lactic acid, etc. The amount of methane produced from the treated cellulose can be up to 70% of the appropriate amount of carbohydrate, dietary pure glucose (see Azzam and Nazer 1993). Lime steaming green grains can also be handled, of course at lower temperatures. It has been shown that optimum results can be achieved by exposing water hygroscopes to 11 pH and 121 ° C (see Patai et al. 1993).

The formation of PAH and methane bacterial growth inhibitors can be achieved at higher temperatures (see Várhegyi et al, 1993; Pa tel et al, 1993), Ez. however, this phenomenon is not observed for pyrolysis used in lime brewing. at temperatures lower than necessary (see Azzam et al. 1993). During pyrolysis

V> · Μ temperatures are so high that biomass decomposes directly into gases such as hydrogen, methane and carbon monoxide, but unfortunately PAH and other pollutants are also produced during the process,

Hereinafter, documents containing the above knowledge will be provided.

Azzam A, M, and Nasr'M. I. (1993) Pbysicohermoehemical pre-treatments Offood Processing waste for anaerobic digestion and biogas fermentation. Journal of Environmental Science and Englneering 23,1629-1849.

Bjerre A. B ,, Ölesen A. B., Fernqulst T, Pioger A ,, Schmidt A, S, (1998) Pretreatrnent of wheat straw using eombined; wet oxidallon and alkaliine hydrolysis re sultlng in convertihle ceMose and hemscellutoses. Bloteehnoiogy and Bloengineenng 49,588577.

Chang V, S., Nagwanl M Holtzappie. T. (1998) Original articles-Llme pretreatment of crop residues bagasse and wheat straw. Applied Biochemistry and Blotechnology Part A-Enzyme Englneering and Blotechnology 74,135-180.

Chang V. S., Barry 8 · ,, Hoifzapple IM. 7 (1997) Isme pre-treatment of svdtchgrass.

Applied Biochemistry and Bleach Engineering Part A-Enzyme Englneering and

Biotechnology 63-65.3-20.

Cureiii N „Fáddá Μ. B., Rescigno A., Rinaldl A.C., Soddu G., Soilal S., Vaccarglu S., Sanjust E., Rinaldi A. (1997) Process alkane / oxidation pre-treatment of wheat straw, Process Biochemistry. 32.635-870.

Patai V., Desal M., and Madamwar D. (1993) Thermo Chemical pre-treatment of water for improved biomethanation. Aoplied Biochemistry and Biotechnoloov 42,8774.

Schmidt A .. S, and Thomsen A. 8. (1998) Optimisatlon of wet oxidatlon pretreatment of wheat straw. Bloresource Technology 64,139-152.

Stróbl, S. K. and Rai, S. N. (1998) Qptimisation of treatment conditions of wheat straw wlth llme: Effect of concentration, moistore confenf and treatment time on Chemical composition and In vlfro digestibility. Animated Eeed Science and Technology 74.5782,

Thomsen Á. B. and Schmidt A .. S. "(1999) Eurther Development of Chemical and Biotechnological Processes for Bio-Ethanol: Optimization of Pre-Treatment Processes and Characterization of Prodrugs, Riso National Laboratory, Roskllde,

Denmark.

Várhegyi, G „Szabó, P., Mok, W. S. L, and Antal, M, J, (1993) Kinetics of the thermo-decomposition of cellulose in sealed vessels by the Journal of Anaiytic and Applied Pyrolysis 26,159-174.

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The traditional use of energy crops is primarily as a solid fuel, whereby the plant is made from sawdust willow wood chips, straw or whole seeds, or the plant is used as fuel for engines, rape oil. Experimentally, eianol is produced from sugar beet and straw (see Parshy; Slms 2001; Gustavsson et al. 1995; Wyman and Goodman 1993; Kuch 1998). In other parts of the world, the use of energy crops is widespread and considerable research is being carried out into them. The use of terrestrial, marine and freshwater plants is well documented (see Gunaseelan 1997; Jewel atal. 1993; Jarwis et al. 1997). According to some studies, anaerobic rotting of energy crops seems to be a competitive solution over other uses of biomass ( see Ohynoweth Ö.P., Owens JM and Legrand R, 2001).

The use of energy crops is strongly encouraged worldwide. Straw processing is already organized in such a way that it is likely to become a widespread practice in the years to come. The use of wood shavings seems to be economical and practicable. However, burning cereal grains raises certain ethical concerns. However, the cultivation of grain crops is essential due to the application of fertilizers and pesticides and the loss of nitrogens in the soil. Nitrogen is also lost during the combustion of biomass.

The following is a list of documents containing the above information.

Beck. J. Co-fermentation of ligands menu and beets as a regenerative © energy. Udiversity of Bohenheim, Dep. Agbcutfural Engtneering and Animál Production. Personal communication.

Cbynoweth, D. P. Owens, J., and Legrand, R. (2001) Renewable mefhane writes anaerobic dicestion ef biomass, Renewable Energy 22.1-8.

Gunaseelan V. Ή. (1997) Anaerobic dentation of biomass for methane production: A revíew. Biomass and Bioenergy 13.83-114,

Gustavsson L „. Bogesson P., Bengt 1, Svenningsson P. (1995) Reducing CO2 emissions by subsfifoting biomass tor fossíi fueís. Energy 20,1097-1113.

Jewell WJ _t Cummsngs RJ, and Richards B. K, (1993) Methane fermentation of energy crops: maximum converslon kinetics and in situ biogas purification. Biomass and Bioenergy 5,281-278,

-11 Jarvls A. Mordberg A., Jarlsvik T. ,, Mathlesen B., and Svensson B. H. (199?) Improvemenf of a grass-clover herege-fed biogas process by the addition of cobalt Btomass and Bioenergy 12,453-460.

Kuch P. J., Crosswbite W. M. (1998) The agrlcu ^ urai regulatory framework and btomass production. Btomass and Bioenergy 14,333-339.

Parsby M. Kaim og eoergiafgroder-analyzer af canon, energi og mUj. Rapport No. 87, Statens dötdbrogs og Rskertokonomiske Institut

Siros R, H, E. (2301) Bioenergy-a renewabie carbon rail. Renewabie Energy 22, 31a?

V f

Wyman C. E. and Goodman 8. J. (1933) Biotechnology for the production of chemicals and matrices for biomass. Applied Biochemistry and Biotechnology 39. 41-59.

Banks C. J. and Humphreys P. N. (1998) The anaerobic treatment of a lignocellulosic substrate offenng littie natural pH bufertog capaciiy. Water Science and Technology 38.29-35.

Colieran E., Wilkie A., Barry M., Fanerty G., O'keily N. and Reynolds P. J. (1983)

One and two slag anaerobic-filter dlgesíion of agrioultural wastes. Thlrd Int. Symp., On Anaerobic Dlgesíion, p. 285-312, Boston MA (1983).

Búgba R. M, and Zbang R. (1939) Treatment of a dairy wastewaler wilh two-stage anaerobic sequencing batch reactor systems-thermopilo verses mesopile operations. Bloresource Technology 88,225-233.

Ghosh S., Ömbregt J, P., and Pspyn P, (1985) Methane production of industrial wastes by two-phase digestion, Water Research 19, 1083-1988.

Han Y, Song S., and Dagus R.R. (1997) Temperature-based anaerobic digestion of wastewater slides. Water Science and Technology 38,387-374.

Krylova N, I ,, Rhabíboulkne R, E., Maumova R. P. Magéi M. A. (1997) Influence of amronium and methods on remodeling during anheerobic treatment of pooitry manure. Journal of Chemical Technology and Biotechnology 70.99-108.

Hansen R, H., Angelidaki I., Ahring B. K. (1998) Anaerobic digestion of swine manure; inhibltion by ammonia. Water Research 32.5-12.

Kayhanian M, (1994) Performance of High-Soil Anaerobic Digestion Processes under Various Ammonia Concentrations, Journal of Chemical Technology and Biofochnology 59,348-352.

Wang Q., Noguehi C. K Kuninobu M., Kara Y Kakimoto K Ogawa. I., and Kató Y. (199?) Influence of hydrauito refentlon tiroeon anaerobic digestton of pre-treated slludge. Siotechnology Techniques 11,105-108.

The systems for collecting carcasses are designed in such a way that the colonies that are authorized to process animal carcasses are registered. Carcasses are used for the production of meat and bone meal, which is traditionally used for animal feed.

Due to the recent SSE outbreak, this practice has been banned by the EC Commission by regulating it, saying that meat and bone meal cannot be used as feed.

The livestock sector and related businesses in Europe have been confronted with the need to find other uses for meat and bone meal, other ways of removing bone meal. However, this is a difficult task due to the austerity measures taken to prevent the spread of BSEprions or other prions that may be present in the flesh or other parts of the flesh.

The use of meat and bone meal and animal carcasses in traditional biogas plants is certainly not recommended and is partly impossible. The processing of the plants áilaltefemek permit such activity is usually about 130 to about 2-3x10 at ^C *

It is carried out under pressure, where the processing time is 20 minutes. Such conditions cannot be guaranteed in conventional biogas plants.

In the following, patents and patent applications in the prior art are described.

DE-3,737,747. Patent No. 5,279,198 describes de-nitrogenizing plants and describes a process. Calcium oxide is added to the fertilizer to remove the ammonia and then absorb the ammonia in an aqueous solution containing hydrochloric acid. Many aspects of the present invention are not found in this document. so ipéidáefi the above document does not mention, in particular, pretreatment, example of alkaline bridge lysis, animal welfare in their place of residence, use of energy plants, absorption of ammonia in sulfur solution, precipitation of phosphorus, biogasification of ciruvite, gas pipelines.

DE-4,201,168. U.S. Pat. No. 4,123,195 discloses a process for treating various organic waste products simultaneously by dividing the waste products into three different fractions containing different amounts of solid components. Before digestion and biogas production, solid

- 13 frackers are homogenized. This description does not include many features of the invention. This means that the above description does not mention pre-treatment, writing, alkaline hydrolysis, animal welfare at their place of residence, use of energy plants, absorption of ammonia in sulfur solution, prevention of phosphorus precipitation, prevention of struvite formation, etc. the use of biogas in local gas production installations or the transport of biogas through gas pipelines.

DE-4,444, Ö 32; U.S. Pat. No. 4,102,125 discloses a plant and process in which slurry is mixed in a first reactor and then vented, and then lime is added to the slurry to produce a pH of 9.5 to remove ammonia. In the second reactor, iron and a polymer-containing salt are added to the slurry to neutralize it and to precipitate solids. This description also does not cover many of the features of the invention, such as pretreatment, <RTI ID = 0.0> (alkaline hydrolysis, </RTI> animal welfare at home, use of energy crops, absorption of ammonia in sulfur solution, leaching of phosphorus, inhibition of localization, etc.) in a gas generating plant or through a gas pipeline,

DE-198,61 S, 083 discloses a process for removing ammonia from digested manure This description does not mention 'many features of the invention,' such as pretreatment, alkaline hydrolysis of rheumatoid oil, animal welfare in their place of residence, use of energy crops, absorption of ammonia in sulfur solution, precipitation of phosphorus, prevention of slruvite formation, mainly use of biogas in local gas generating plant or biogas pipeline

EP-0,286,115. U.S. Pat. No. 4,123,125 discloses a process for the production of biogas by mixing with manure fatty acids or fatty acid compounds. This specification also fails to mention many of the essential features of the present invention, such as pretreatment, such as alkaline hydrolysis, animal welfare at home, use of energy crops, absorption of ammonia in a sulfur solution, precipitation of phosphorus, prevention of sphruffite formation, in a local gas production plant or in a biogas plant

EP-0,351,922. U.S. Pat. No. 4,123,125 discloses a plant and process for removing ammonia, carbon dioxide and phosphate from liquid manure. A «♦ <

** manure is transported from the plant to the plant by tanker, where the slurry is treated with hot air to remove ammonia and carbon monoxide. The remainder of the slurry is heated and lime is added to give a p H value of 10-11, thereby extracting additional ammonia and producing calcium phosphate. The extracted ammonia is absorbed in an acidic solution by the formation of an ammonium salt. The resulting slurry is dried and used as fertilizer. The solids are separated from the slurry by a decanting centrifuge. This specification also fails to mention many of the essential features of the present invention, such as pretreatment, alkaline hydrolysis of animal, animal welfare, use of energy crops, absorption of ammonia in sulfuric solution, precipitation of phosphorus, further formation of struvite. use in a local gas production plant or for the removal of biogas through gas pipelines.

U.S. Patent No. 2,100,123 describes a plant and process in which liquid manure is purified. The organic components are decomposed and the precipitated solids are removed by a decanter centrifuge. Acid is added to the liquid and then spread on the ground or further purified by venting and removing ammonia. The purified liquid is sent to a water treatment plant. This description also fails to mention many of the essential features of the invention, such as alkaline hydrolysis, animal welfare in the home, pre-removal of ammonia, use of energy crops, prevention of struvite formation, and semi-use of biogas for local gas production. equipment or the removal of biogas through gas pipelines.

No. FR-2,576,741. U.S. Pat. with which biogas can be produced by digesting liquid manure. The slurry is treated with lime and the precipitated components are removed. Many important features of the invention are not mentioned in this specification, such as pretreatment, alkaline hydrolysis, for example, use of energy crops, phosphorus precipitation, prevention of struvite formation, use of biogas in a local gas generator or biogas pipeline.

© 8-2,813,170. U.S. Patent No. 4,123,125 discloses a plant and process for the production of biogas. In the first reactor, the organic material is acidified and the solid fraction is removed. The liquid fraction is fed to a second reactor of egv, where anaerobic decomposition occurs with methane production. Also, this description does not mention many of the essential features of the invention, such as:

«♦ ..« «♦ *.« · <* ♦ «Λ ♦« * *

- 15treatment, hydrolysis of biofuels, animal welfare in their place of residence, use of energy crops, removal of ammonia, phosphorus acidification, prevention of cerebrovascular accident, use of biogas in a local gas generator or biogas pipeline

DE 19,644,613. U.S. Pat. No. 4,123,125 discloses a process for producing fertilizers from organic fertilizers. To the slurry are added materials from biogas production, as well as calcium oxide or calcium hydroxide. The extracted ammonia is collected. This description omits many of the essential features of the present invention, such as pretreatment, alkaline hydrolysis, animal welfare, use of energy crops, phosphorus precipitation, prevention of struvite formation, and the like. in a gas-generating plant or in a biogas pipeline.

DE-19,828,889 discloses the co-digestion of harvested plants and organic waste with biogas production. The essence of this process is to homogenize the starting material and then to erase it. The above description is also; does not include many of the essential features of the present invention, including: pretreatment,> idid <alkaline hydrolysis, animal welfare at home, use of energy vents, phosphorus acidification, prevention of slurry formation, sjX, and use of biogas for local gas production

V »· in a plant or through a biogas pipeline.

U.S. Patent No. 4,041,182. U.S. Pat. No. 4,123,125 discloses a process for the preparation of animal feed from organic waste. This description does not mention many of the essential features of the present invention, such as the following. pre-treatment,

Examples include alkaline hydrolysis, animal welfare in their habitat, use of energy crops, phosphorus depletion, prevention of cerebrovascular accident, etc., and semi-use of biogas in a local gas generator or through biogas pipelines.

U.S. Pat. No. 4,100,023. U.S. Patent No. 4,123,125 describes a plant and process for producing methane and fertilizers. In the first reactor, the homogenized material is aerobically degraded. The heated second reactor undergoes anaerobic digestion with biogas production. Fertilizers are produced in liquid form. This description also fails to mention many of the essential features of the present invention, including: pretreatment, alkaline hydrolysis of elephant, animal welfare at home, use of energy crops, removal of ammonia, phosphorus removal, struvite «# ♦ * χ ♦ * -» « * * ««> ·> 4 ·. X ·>

.... 16 ....

and the use of biogas in local gas production facilities or the removal of biogas through gas pipelines.

U.S. Patent No. 4,329,42b. The patent describes a plant for anaerobic digestion and describes the method of digestion of various green plants and their producers using biogas. The operation of the plant is based on the digestion by mesophilic or thermotilic anaerobic bacteria. This description does not overlook many of the essential features of the present invention, such as the following: pretreatment, live / alkaline hydrolysis, animal welfare at home, use of energy crops, removal of ammonia, leaching of phosphorus, localization of gasses, equipment or biogas draining gas pipelines help.

U.S. Patent No. 4,579,854. The patent discloses a process and a process for the production of biogas from organic materials. The solids are hydrolyzed, acidified and then removed, A. This specification also fails to mention many of the essential features of the present invention, including pre-treatment, alkaline hydrolysis of the oil. , animal welfare in their place of residence, use of energy crops, removal of ammonia, phosphorus precipitation, prevention of struvite formation, etc., and use of biogas in local gas production facilities or biogas removal by gas pipelines,

U.S. Patent No. 4,888,250. U.S. Pat. No. 4,123,125 discloses a process in which ammonia is removed from the liquid fraction by aeration. This description also fails to mention many of the essential features of the present invention, such as, for example, pretreatment, hydrolysis of algae, animal welfare at home, use of energy crops, phosphorus deposition, and inhibition of struvite formation. and the use of biogas in the wall of a local gas generator or the removal of biogas through gas pipelines.

U.S. Pat. No. 4,780,454. The patent describes a plant for the anaerobic digestion of organic fertilizers and the use of biogas produced in the process. The operation of the plant is based on the decomposition of mesophilic or thermotilic anaerobic bacteria by a stationary gas generator equipped with a generator. The above description also does not mention many of the essential features of the invention, such as pre-treatment, alkaline hydrolysis of jealid, animal welfare in their place of residence, use of energy crops, removal of ammonia, phosphorus.

17, the prevention of struvite formation, the use of biogas in a local gas generator or biogas via gas pipelines.

U.S. Pat. No. 071.5-9. U.S. Patent No. 4,123,125 describes a method for treating organic fertilizers. Water is added to the fertilizer and the mixture is acidified. The liquid is removed by steam generation and the resulting steam is condensed in another reactor and treated anaerobically to produce biogas. The digested liquid is then treated with an aerobic process. The above description does not mention many of the essential features of the present invention, such as: pretreatment, alkaline hydrolysis of j-beams, animal welfare at home, use of energy crops, removal of phosphorus, prevention of struvite formation, use of biogas in a local gas generator or removal of biogas by gas pipelines,

US-S.296 ', U.S. Pat. U.S. Pat. No. 4,123,125 discloses a method for treating organic fertilizers and other organic components. The organic waste is digested and then disposed of, followed by denitration. Numerous essential features of the present invention are not mentioned in this patent, such as pretreatment, such as alkaline hydrolysis, animal welfare, energy crops, ammonia recovery, phosphorus precipitation, and struvite formation. in a local gas generator or through biogas pipelines.

U.S. Patent No. 5,398,258. U.S. Pat. No. 4,123,125 discloses a process for producing biogas from semi-solid and solid organic waste. However, this description does not overlook many important features of the present invention, for example. on pre-treatment, alkaline hydrolysis for example, animal welfare in their place of residence, use of energy crops, removal of ammonia, leaching of phosphorus, prevention of struvite formation, and use of biogas in local gas production facilities or biogas pipelines

U.S. Patent No. 5,494,587. U.S. Patent No. 4,123,125 to Catalyst discloses the catalytic treatment of fertilizers in which the concentration of nitrogen is reduced. This description also fails to mention many of the essential features of the present invention such as pretreatment, such as alkaline hydrolysis, animal welfare at home, use of energy crops, removal of ammonia, phosphorus leaching, prevention of struvite formation, and use of biogas in local gas production plants or biogas help.

U.S. Patent No. 5,525,229. U.S. Patent No. 4,123,125 discloses a general process for the anaerobic digestion of organic materials using both static and mesophilic conditions

U.S. Patent No. 5,598,590. U.S. Pat. No. 4,123,125 discloses the separation and treatment of liquid and solid organic waste, followed by separation of the two fractions. The liquid fraction is digested to produce biogas and the precipitated solid components are then removed and partially recycled. The solid fraction is treated with an aerobic process to produce compost, fertilizer or animal feed. Some of the biogas produced contains methane and - carbon dioxide is reused to reduce the pH of the liquid fraction by absorbing the carbon dioxide. The solids are precipitated from the liquid fraction by a decanter centrifuge and the pH is 9-10. The waste water can be used to clean the Stables. The foregoing description does not mention many of the essential features of the present invention, such as pretreatment, alkaline hydrolysis of ephalone, animal welfare at home by the use of straw, use of energy crops, removal of ammonia prior to biogas production, precipitation of phosphorus, struvite formation. ,> etc., as well as the use of biogas in a local gas production plant or the removal of biogas via gas pipelines.

U.S. Patent No. 5,816,183. U.S. Pat. No. 4,123,125 discloses a method for treating organic fertilizers using nitrogen to produce the fertilizer. Diluted manure is supplemented with CO ₂ and / or CaS-Q ₂ to remove ammonia from the manure. This description does not mention many of the essential features of the present invention, such as pretreatment, folate effluent hydrolysis, animal welfare at home using straw, use of energy crops, removal of ammonia prior to biogas production, trapping of phosphorus. , the prevention of struvite formation, the use of ptbl, and the use of biogas in a local gas generator or the removal of biogas via gas pipelines.

U.S. Pat. U.S. Pat. No. 4,123,125 discloses a method for treating organic fertilizers using nitrogen to make fertilizer by more or less centrifugation. Numerous essential features of the present invention are not mentioned in the said patent, such as pre-treatment, hydrolysis of falpel, alkaline animal welfare through the use of straw, use of energy crops, removal of ammonia prior to biogas production, precipitation of phosphorus, ,> tb 'furthermore, use of biogas in a local gas-generating installation or through biogas pipelines.

US-S, 670.04? s. U.S. Pat.

U.S. Patent Nos. 133-5,681,481; U.S. Pat. No. 5,783,073; and U.S. Pat. No. 851,404; U.S. Pat. Lime is added to the slurry so that the pH is at least 12 and the resulting mass is kept for at least 5 ° C for 12 hours. Ammonia is removed and either released into the atmosphere or recycled to the system. As a decanter centrifuge, suitable for mixing this slurry is a so-called centrifuge. a preheating chamber can be used to keep the slurry in a liquid state. The slurry is then spread to the ground. None of the above-mentioned descriptions contain many of the essential features of the present invention, such as pretreatment, dietary alkaline hydrolysis, animal welfare at home by the use of straw, use of energy crops, removal of ammonia prior to biogas production, phosphorus precipitation, slurry formation, jtbC also includes the use of biogas in a local gas production plant or the removal of biogas through gas pipelines.

U.S. Pat. No. 5,746,919. U.S. Pat. Both reactors produce methane. Neither will this description. mention is made of a number of important features of the present invention, such as pretreatment, hydrolysis of moths, animal welfare at home by the use of straw, use of energy crops, removal of ammonia prior to biogas production, precipitation of phosphorus, prevention of struvium formation, or the removal of biogas through gas pipelines.

Patent Application No. 03-6,773,526 discloses a process in which liquid and solid organic waste is digested first by a mesophilic process and then by a productive process. The solid components are hydrolyzed and acidified. Also, this description does not mention many of the essential features of the present invention, such as the following; pretreatment, alkaline hydrolysis of buffalo, animal welfare at home using straw, use of energy crops, removal of ammonia before biogas production, phosphorus precipitation, struvite formation fc

- 20 blocking. §lake.,. and use of biogas in local gas generating installations or through gas pipelines ·

U.S. Patent No. 5,782,950. U.S. Patent No. 4,123,125 discloses the digestion of biological waste by homogenization, aeration, and heating of the mass, The waste is fractionated into liquid and solid fractions, The solid is composted, The liquid fraction is anaerobic mesophilic, and the process is digested, water is recycled from the biogas production reactor to the homogenization process. The waste water from the biogas production reactor is treated in a water purification plant. The above description does not mention many of the essential features of the present invention, such as the following; pretreatment, for example, alkaline hydrolysis, animal welfare in their place of residence, use of energy crops, removal of ammonia prior to biogas production, phosphorus precipitation, prevention of struvite formation, and use of biogas in a local gas generator or biogas pipeline.

U.S. Patent No. 5,853,450. U.S. Patent No. 4,123,151, issued December 6, 1992, describes a process for making pasteurized compost from organic waste and green plant materials. The pH of the organic material is raised to 12 and the temperature raised to above 55 ° C. When green plant material is added to the organic matter, the pH is lowered to 7 ... 9.5. The mixture is then rot. The above description does not include many of the essential features of the present invention, including the following; pretreatment, such as alkaline hydrolysis, animal welfare in their home, use of energy crops, removal of ammonia before blogging, precipitation of phosphorus, prevention of struvite formation, etc., and use of biogas in a local gas generator or biogas pipeline.

U.S. Patent No. 5,863,434. U.S. Pat. Also, this description does not mention many of the essential features of the present invention of pre-treatment, ipefdstfi | alkaline hydrolysis, animal welfare at their place of residence, use of energy crops, removal of ammonia prior to biogas production, phosphorus precipitation, prevention of struvite formation, and use of biogas in local gas production facilities or biogas pipelines.

U.S. Pat. U.S. Pat. No. 4,102,125 discloses a method and system for treating organic fertilizers with ozone to form aerobic and anaerobic zones in the material. This description does not overlook many of the essential features of the present invention, such as pretreatment, alkaline hydrolysis of animals, animal welfare in their habitat, use of energy crops, removal of ammonia prior to biogas production, precipitation of phosphorus, prevention of struvite formation, -ib. as well as the use of biogas in a local gas production plant or the removal of biogas through gas pipelines.

U.S. Patent No. 6,171,499. U.S. Pat. No. 4,123,125 discloses a process for rotating household and industrial waste. The waste is anaerobically digested while producing biogas, where the biogas is used in a gas turbine in combination with natural gas. The digested material is dehydrated and the resulting slurry is sent to an incinerator. This description also fails to mention many of the essential features of the present invention, such as pretreatment (e.g., alkaline hydrolysis, animal welfare at home, use of energy crops, removal of ammonia prior to biogas production, precipitation of phosphorus, prevention of struvite formation). furthermore, the use of biogas in a local gas generating plant or the removal of biogas via gas pipelines

WO 84/00038. U.S. Patent No. 4,123,125 discloses the production of biogas and gas-stabilized and stabilized fertilizers. Thermophilic degradation takes place in an internal reactor, while mesophilic degradation takes place in an external reactor. The above document does not mention many of the essential features of the present invention, such as pre-treatment, such as alkaline hydrolysis, animal welfare at home, use of energy bulbs, removal of ammonia prior to biogas production, phosphorus precipitation, struvite formation, pfb. as well as the use of biogas in local gas production installations or the removal of biogas through gas pipelines.

WO 89/00548. U.S. Pat. No. 4,123,125 describes the use of Ca-ions and Mg-ions in biogas production. Metal ions prevent foam formation. This description does not neglect many of the essential features of the present invention, such as: pretreatment, live (alkaline hydrolysis, animal welfare at home, use of energy crops, removal of ammonia before biogas production, precipitation of phosphorus, prevention of struvite formation). , ptb ',, furthermore the use of biogas in a local gas production plant or the removal of biogas via gas pipelines.

WO 91/02582 discloses a plant and process for the production of gas, which purification of the gas eliminates the release of harmful compounds into the environment. The above document also does not mention many of the essential features of the present invention, such as:

pre-treatment, - alkali hydrolysis of food, animal welfare in their home, use of energy crops, removal of ammonia prior to biogas production, phosphorus precipitation, prevention of struvite formation, and the use of biogas in local gas production facilities or biogas pipelines.

WO 99/42423. A process and a plant for the production of biogas are described in U.S. Pat. No. 4,123,123. The fibers and particles in the fertilizer are composted and the liquid fraction is anaerobically decomposed and the nitrogen is extracted therefrom. The salts of phosphorus and potassium are used in fertilizers through reverse osmosis. This description also fails to mention many of the essential features of the present invention, such as pretreatment, φόΗόηál alkaline hydrolysis, animal welfare at home, use of energy crops, removal of ammonia prior to biogas production, precipitation of phosphorus, prevention of struvite formation, use of biogas in a local gas production plant or the removal of biogas through gas pipelines.

A. www.lgb.fbg.de/0wbio/en/Manure.en.htmi describes the process by which biogas can be produced from organic fertilizers. The solid fraction derived from gasphosphinated organic fertilizers is used to make a composite. Nitrogen is collected from the liquid fraction and utilized as fertilizer. A decanting centrifuge is used to separate the solid components from the mixture. The cited document also does not mention many of the essential features of the present invention, such as of: pre-treatment, - ^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^ ^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^ .

The btbp: //ne.ra.ceeeta.pt/ímages/ukb; o ... mass.htm web site describes the production of biogas by anaerobic digestion. A decanter centrifuge can also be used in the system. The said website also does not mention many of the essential features of the present invention, such as pretreatment, ipéMafe alkaline hydrolysis, animal welfare at home, use of energy crops, removal of ammonia before biogas production, precipitation of phosphorus, formation of struvite. as well as the use of biogas in local gas production installations or the removal of biogas through gas pipelines.

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· -23

The www. Biogas. ch / He / meme rr, htm describes your online options for reducing a mixture of solid components. The said document mentions the use of rotary disk reactors, fixed film reactors, ultrafiltration and reverse osmosis as possible solutions. However, this document does not mention many important features of the present invention, such as:

pretreatment, alkaline hydrolysis, animal welfare in their home, use of energy crops, removal of ammonia before biogas production, phosphorus precipitation, prevention of struvite formation, §fb '.' ₍ furthermore, the use of biogas in local gas generating installations or the removal of biogas through gas pipelines.

The www.biopas.ch ^ e / grasbaslhtm website describes the anaerobic digestion of silage and organic manure with biogas production. Two procedures are described;

1. Sheaf plants are chopped into 1-3 cm vengeance pieces and fed into a liquid fraction containing organic fertilizer. The mixture rothasztják at 35 ^o C. 2. Organic fertilizers and silage plants are treated by dry digestion without adding any additional liquid. The above document also does not mention many of the essential features of the present invention, such as (e.g., pre-treatment, e.g. alkaline hydrolysis, animals). well-being at their place of residence, use of energy crops, removal of ammonia before biogas production, phosphorus precipitation, prevention of struvite formation, etc., and use of biogas in local gas generating installations or biogas pipelines.

The www.feiogas.ch/Hg/2etede.htm website describes the production of biogas. The organic waste is hydrolysed and acidified in a rotary screen drum, from which the liquid fraction is continuously discharged to a plant in which anaerobic digestion with biogas production is carried out. This document does not mention many important features of the present invention, such as the following; alkaline hydrolysis of animals, animal welfare in their habitat, use of energy crops, removal of ammonia prior to biogas production, phosphorus precipitation, prevention of struvite formation, use of biogas in local gas generating equipment or biogas pipelines.

The object of the present invention is the new utilization of energy crops, namely the anaerobic digestion of energy crops and organic fertilizers in large-scale biogas plants. The invention further relates to slurry separation, that is, to refining nutrients in organic fertilizers.

The objectives of the present invention are achieved by the use of a process for reducing the number of viable microbial organisms and / or prions in organic materials, which process comprises:

i) collecting organic material containing solid and / or liquid parts;

11} On organic matter, we do the following:

a) the organic material is biolysed by high-pressure lime cooking at a temperature between 10 ° C and 220 ° C, where the lime is cationic hydroxy and / or calcium oxide, and then

b) removing the ammonia from the organic material treated with high pressure lime;

wherein the lime added to recover the ammonia and to disinfect the organic matter precipitates from its dissolved orthophosphates;

(ii) producing processed deer material which contains reduced amounts of viable microbial organism and / or prion; and arc) feeding the processed grain material into a biogas-producing digester in which the processed organic material is digested and thereby produced.

The objects are further achieved by implementing a biogas plant which produces the biogas by anaerobic digestion of processed organic material containing solid and liquid parts. The plant comprises at least the following units:

I) an extraction tank for extracting ammonia from the organic material treated in the high-pressure lime digester unit, wherein the extraction tank is connected to an absorption unit for absorbing and condensing the recovered ammonia,

II) a digestion tank for the anaerobic digestion of organic material treated in the high-pressure lime digestion unit, which results in digestion production, and

Hl) a high-pressure lime digestion unit for hydrolyzing the organic matter, wherein the high-pressure lime-digestion unit and the extractor are connected such that the organic material treated with the high-pressure lime-digestion unit can be led from the high-pressure lime digestion unit to the that the organic matter treated by high pressure lime and de-ammonia can be transferred from the extraction tank to the biogas digestion tank, and wherein the high pressure lime digester and the extraction tank are further connected to each other so that the recovered ammonia is extracted from the high pressure steam can be transported to a container and absorbed in a brain absorption unit.

The present invention is suitable for the co-digestion of animal carcasses, meat and bone meal and organic fertilizers / energy plants, thus providing a solution for the disposal of animal waste while processing animal waste and plants, organic fertilizers, as fertilizers.

The present invention allows the cultivation of perennial fodder plants, such as sugar beet, maize, alfalfa, etc., for all crops which produce a higher dry matter per hectare than cereal grains. Fodder plants can also be used as green plants, and can be used immediately The invention makes it useful to cultivate energy crops in remote areas by the method of sehnti.

Biogas production based on the present invention is expected to become competitive in the future for natural gas production, thereby making it commercially attractive, but not expediently subsidized. In our opinion, Danish energy production will cover a significant part of Danish energy consumption and will be in the same order of magnitude, using about 150 Faii per year. In addition, this type of energy production is beneficial for the environment, animal welfare and food safety. .

Parsby estimates that energy crops, especially grain cereals, can produce between 50 and 80 PJ a year. This requires 150,000 hectares in the short term and 300,000 hectares in the long term. If, on the other hand, it is assumed that sugar beet, which produces 15 tonnes of dry matter per hectare, is co-digested in biogas plants, energy production can be up to about 100 PJ / year. This would add the energy from the organic fertilizer from the co-trothastoft, which would be about 25 PJ. With the cultivation of new varieties of sugar beet, the dry matter yield could be significantly higher than the present level, ie around 25 tonnes per hectare,

SUMMARY OF THE INVENTION The present invention relates to a combination of processes that enable enhanced biogas production, ammonia extraction and further potential utilization, and the processing of digested and extracted residues, such as wastewater.

«X

An essential feature of the present invention is the integration of simple and robust processes into a single process. The invention enables simple and robust power generating plants to be realized which are excellent in power generation! and have economical features compared to conventional plants. The energy generating plants implemented by the present invention can also be integrated into the Livestock and Agriculture Management Systems,

One embodiment of the method of the invention is to prevent the spread of infections, as well as animal microbial and parasitic pathogens, Campylobacter, Saimonyolia, Yersinia, Acarls and other similar microbes and parasitic organisms in the air and in the soil. In this way, we reduce the risk of human infection.

The invention makes it possible to reduce the number of BSE prions in organic fertilizers, feed, slaughterhouse waste, meat and bone meal, and so on. This is achieved by a combination of pretreatment and digestion. As a result, the invention provides an opportunity for animal carcasses, slaughterhouse waste, gfb. that is, it is possible to use nutrients in animal carcasses as fertilizers. In animal carcasses, meat and bone meal, organic fertilizers, animal feed, slaughterhouse waste, <6. reducing the number of BSE prions present and / or completely destroying them is essential for such treatment of organic waste. The process of the invention provides an alternative solution for the processing of dead animals in central plants (which is currently prohibited by EU advances) and for the preparation of various products, mainly for the production of meat and bone meal.

One embodiment of the process of the present invention is suitable for the selection of the main nutrients, organic nitrogen and phosphorus in organic fertilizers and for processing these nutrients into commercial grade fertilizer products.

Another embodiment of the present invention allows the production of large amounts of biogas from a variety of organic materials, including all possible animal manure, energy crops, plant residues, and other organic wastes.

Another embodiment of the present invention maintains animal welfare and health at optimum levels when they are in pens. They are in stables,.

while the. it reduces emissions of dusts and gases, such as ammonia. This is achieved by flushing the C-Sj animal settlements with infertile water and refluxing the infertile water.

A further preferred embodiment of the invention combines all of the earlier embodiments.

Other possible preferred embodiments of the invention include one or more of the foregoing variants.

The invention will now be described in more detail with reference to the drawing. In the drawing:

Figure 1 illustrates one embodiment of the system of the present invention;

Figure 2 illustrates another possible embodiment of the system according to the invention;

Figure 3 illustrates another possible simplified version of the system according to the invention;

Figure 4 is a variant of the system of Figure 3 in which potassium is not precipitated;

Figures 5 and 6 illustrate a flow diagram of a further embodiment of the system according to the invention.

In the embodiment of the system according to the invention, as shown in Figure 1, animals, in particular domestic animals, are exemplified. manure from pigs, cattle, lambs, goats, sheep and / or poultry, pigs, turkeys, ducks, geese, 101, preferably in slurry form, from a first pretreatment tank and / or a second pretreatment tank forward to one or both.

The operation of the system according to the invention is based on the principle that manure, preferably in the form of slurry and containing manure containing water, e.g. to a first pretreatment vessel, which is preferably an extraction vessel 102 in which ammonia is removed by addition of an additive, for example CaH and / or Ca (OH) ₂ , to the material in the vessel, CaO and / or Ca (OH) ·? However, the addition of compound to the slurry can also be done before the slurry is introduced into the first treatment vessel, i.e. the extraction vessel 102.

At the same time as the addition of CaO and / or Ca (OH) ₂ or at a later time in the pretreatment tank containing the extraction tank, nStrogen / ammonia

Extraction and / or heating of the slurry and expediently absorbing the recovered nitrogen or ammonia before storing it in a separate container 111 for the brain. The nitrogen-containing recovered ammonia is absorbed in the ammonia-absorbing column in the first pretreatment tank, preferably in an extraction tank 102, before being transferred to another tank for storage.

Organic materials which are difficult to digest with mycobacterial organisms during anaerobic digestion are preferably pretreated in a second pretreatment tank before being introduced into a first pretreatment tank containing the above-mentioned extraction tank. Such organic materials typically include: significant amounts of, for example, cellulose and / or hemicellulose and / or lignin, preferably containing more than 50% by weight of cellulose and / or hemicellulose and / or lignin, based on the dry weight of the organic material, e.g. , fodder plants, including maize, vegetable waste or other solid organic matter. The nitrogenous ammonia is subsequently removed from the pre-treated organic material,

The slurry is subjected to thermal and alkaline hydrolysis in both the first and second pretreatment tanks. However, the temperature and / or pressure is substantially higher in the second pretreatment vessel, which is therefore desirable to provide a closed system capable of maintaining high pressure.

Finally, the aforementioned pretreated slurry is preferably introduced into at least one productive digestion tank 108 and / or at least one field biogas producing digestion tank 106. The slurry is then anaerobically digested simultaneously in the two digestion tanks 106 to form a biogas containing which in some cases also contains smaller amounts of carbon dloxldof. The biogas-producing digestion tanks 108 are preferably implemented as part of power generation plants that are capable of generating greater amounts of organic material than hitherto.

The biogas can be fed to a gas engine and the energy from this engine can be used to heat the recovery tank. However, biogas can also be removed through a commercial biogas pipeline network that transports biogas to households and industrial users.

The material remaining in the anaerobic digestion, which remains in the form of a slurry containing solid and liquid material, is preferably conveyed to at least one decanter centrifuge 107 which separates the solid and liquid materials. This separation is the

",; *** ♦. · ♦ * *>

results in at least a semi-solid fraction consisting almost exclusively of tungsten; and a tertiary solid fraction containing more than 50% by weight of phosphorus. In the same step, or in a separation step with another decanting centrifuge 108, another, at least partially solid fraction is prepared which preferably contains almost exclusively potassium. This potassium fraction is at least a semi-solid fraction which preferably contains more than 50% by weight of potassium. Said fractions, which after a drying step, after a spray drying or slurry drying, are prepared in granular form and stored in tanks, preferably of commercially acceptable phosphorus and / or potassium, suitable as fertilizers 110. Such a fertilizer 110 can be applied to the plants or to the fields. Liquid formed during separation of the decanter by centrifugation. tailings can also be discharged to arable land, recycled back to stables or stalls 101, or taken to a sewage treatment plant.

In another embodiment of the system of the present invention, the first pretreatment tank is filled with organic materials stored in silage tanks 104 containing rotable organic materials. While delivering such organic materials to the first pretreatment tank, we produce anaerobic digestion crop! 115 digestion tanks suitable for removing gases from the silo. In addition, straw and plant debris from agricultural soils are also transported to the stables or sheds 101, and later to the first pre-treatment tank 102 and / or the second pre-treatment tank,

The system shown in Figure 2 consists of the following elements: 201 sheds or stables, extraction tank 202, high-pressure lime digestion unit 203, silo tanks 204, field 205, digestion tanks 208, 213, decanter centrifuge 208, manure 208, tanks 210, 211 and 214 waste water tanks,

The system shown in Figure 2 is substantially the same as the system shown in Figure 1, except that after separation by decanting centrifuge 207, only the phosphorus is collected. The water in the form of waste water is collected in a separate reservoir 214 for further purification, in which nitrogen, odors and most of the remaining solids are removed. This step can be done by aerobic digestion. At this step, potassium may even be separated from the liquid.

φ φ

-30Α Figure 3 shows a system illustrating a simplified solution for a combined biogas production and sludge removal system. This version of the system according to the invention consists of the following elements: 301 pens or stables, 302 extraction tanks, 303 high pressure lime digesters, 304, 305 decanter centrifuges, 303, 309, 310 tanks and 311 sludge tanks,

In this version of the system, no biogas producing rotting tanks are used and the solids resulting from the pre-treatment of the extraction slurry in one or two pretreatment tanks are introduced into one or more decanter centrifuges 304, 305 after the removal of nitrogenous ammonia. The ammonia was collected in a separate container 308. Decantation yields at least a semi-solid prime fraction, a potassium-containing fraction, which is collected in tanks 309 and 310,

The system shown in Figure 4 consists of the following elements: 401 pens or sheds, extraction tank 402, high pressure lime brewing unit 403, decanter centrifuge 404, tanks 408, 400, field 405, wastewater 408, and tanks 407.

Following separation of this system by decanter centrifuge 404, potassium is not selected, as is the case with the system shown in Figure 3. However, potassium can be separated from the waste water collected later.

Figures 5 and 8 illustrate another embodiment of the system of the present invention. The individual components shown in the figures are described in more detail below. The invention will now be described in several respects.

The disinfection system is a first device, namely a house or barn for raising domestic animals, pigs or deer and / or a second device, in particular a means for removing ammonia and pretreating the slurry and / or a third device, in particular a slurry it has a power generating plant capable of producing more energy than before.

Preferably, the system consists of a barn, an extraction tank and a biogas production reactor, but the system may also include other elements such as a device for adding Ga0 or Ca (OH) r to the slurry, an absorption column containing ephafe / sulfuric acid. , may also include an ammonium concentrate storage tank and a slurry storage tank.

The biogas produced can be used for the desired use of electricity and heat in a gas-powered engine and generator, where the current is preferably in an electric network.

While the heat is preferably used for heating, slurry and / or barn heating, the power generating unit of the present invention has excellent performance in terms of the amount of energy produced per unit mass of material treated in the unit. Excellent performance is achieved by pretreating the material to be digested and removing the ammonia from the slurry prior to anaerobic digestion, where the slurry can be organic fertilizer or other organic material.

Advantages of the System of the Invention One of the key features of the system of disinfection according to the invention is a pre-treatment comprising the following pre-treatment steps:

Pretreatment of the slurry removed from the stable may include one or more of the following steps; 1) removal of ammonia, 2) hydrolysis of organic material, 3) disinfection of slurry, 4) reduction of foam formation, 5) removal of flakes, 6) precipitation of phosphorus and 7) prevention of struvite formation.

The essence of the treatment is to transfer the slurry from the first device to an extraction tank where the ammonia is extracted by adding CaO or Ca (OK) ₂ , then the extracted ammonia is heated and absorbed on a column before being stored in a separate tank. The slurry is simultaneously subjected to thermal and alkaline hydrolysis, preferably using a limestone digester. methane and, to a lesser extent, carbon dlexide. The biogas is fed to a gas engine and used to heat the extraction tank. The electricity produced in this way is sold to the electricity supplier.

Because straw and optionally sawdust represent a significant part of the litter from cattle stables and poultry farms, these fertilizers require special pre-treatment before they can be optimally processed in a biogas plant. Such pretreatment is preferably high pressure cooking of lime. Deep litter treated with this technology can produce methane much more efficiently, and biogas production will also increase. In addition, we ensure that uric acid and urea are homogenized to ammonia, and that proteins and other materials are dissolved. In this way it is assured that. inorganic nitrogen from litter is collected in the form of a concentrate of nitrogens as a result of the ammonia extraction process.

By the process of the present invention, considerably more nitrogen is present in arable crops in dreams and in poultry manure. It is estimated that the potential processing efficiency can be increased to about 90% compared to other fertilizers that are treated in the biogas production and sludge separation plant of the present invention.

In some cases, it may be appropriate to feed the poultry manure into the first crop or field reactor before transferring it to the extraction tank. The feasibility of this step depends, on the one hand, on the quality of the fertilizer and, on the other hand, the extent to which the uric acid is degraded by the two different treatments. The experience gained during certain times of operation of the plant may clarify this issue. It is essential to maintain the versatility of the plant so that all kinds of fertilizers and energy crops can be processed.

The technical design of the system according to the invention is relatively simple since the biomass is conveyed by a conveyor screw made of stainless steel and acid-proof steel with a loosening device to a limestone boiler, where the mass is heated by injection of steam to 1802 ° ^C. A pressure of 11.6 x 1 &lt; RTI ID = 0.0 &gt;

The unit should be implemented 1Ö0-20Ö temperature and high pressure suitable for preparation of C ^n. In this way, it is possible to adjust the treatment parameters for the various biomasses to be digested in the plant according to the invention, taking into account energy consumption, germination and other technical parameters.

Foaming is a common problem in biogas plants. One convenient way to control the formation of foam in such plants is especially for large amounts of biomass, particularly biomass from energy crops - rapeseed oil; application, which, in addition to controlling the formation of foam, also serves as a basis for the formation of methane gas. Ca-ions are also very effective in controlling foam formation, as are many other salts. According to the invention! in the system, Ca (OH) ₂ and / or CaO are preferred agents for controlling foam formation, which are also advantageous for their other effects mentioned above. The addition of Ca ions to the slurry thus improving the efficiency of anaerobic digestion.

In view of the foregoing, if high gas formation requires control of foam formation and / or flocculation during the process, calcium and / or rapeseed oil may be directly introduced into the digestion tanks. Addition of Ca (OH) _s or CaO also results in the precipitation of bicarbonates, such as CaCO ₃ , thereby reducing the concentration of CO _S in the solution and in the gas phase, which reduces the rate of foaming through a decrease in carbon dioxide release.

Addition of Ca {OB} ₂ or CaO, as well as removal of ammonia and disinfection of the slurry also contributes to the precipitation of ortho-phosphates such as soluble phosphorus (PO /). These phosphorus hollows, together with other flakes, float in the sludge. The use of calcium also leads to a limited reduction in chemical oxygen demand (COD); which means that calcium precipitates other salts than orthophosphate.

Irrespective of the difference in chemical characteristics between the various organic wastes, it is assumed that a simple heat treatment, in particular combined with alkaline hydrolysis, is a. allows for the production of larger quantities of gas. In addition, the combination of high temperature and high pH during pretreatment is also likely to result in more effective disinfection of the organic material, compared to purely anaerobic digestion, whether it is of a crop or mesophilic rot.

It should be noted that the Danish Ministry of Environment and Energy, No. S23, rendeiete requires a supervised disinfection 1 hour 'at 70 ^c C; needs to be done. In view of this, it is desirable for the system of the invention to disinfect at 70 ° C for one week prior to the subsequent two anaerobic digestion, the natural and mesophilic digestion, which, in our opinion, completely excludes all animal and / or human microbial and zoonotic pathogens. survival. With this treatment, the SSE prions are also completely destroyed or at least significantly reduced in number.

Ultimately, all infectious organisms in the slurry are destroyed and not released into the environment when the fertilizer is applied to the soil. In this way, it is also possible to rinse the first device, i.e. the animals' dwelling, with the digested slurry in order to keep them clean, thus preventing the animals from infecting each other. It is also possible to use water, carcasses to clean you and your pens, and to release water to the atmosphere without releasing odorous, dusty or infectious substances into the air. This is made possible by the fact that slurry containing excess water cannot be stored for a specified period where fertilization of the land is permitted. The nitrogen-free slurry can be applied to the land throughout the year.

In the process of the invention, pretreatment and disinfection of the slurry is essential in order to allow subsequent application of the slurry to the fields.

It will be appreciated that the present invention has many different aspects, which are patentable inventions, alone or in combination. Hereinafter, the various stand-alone units, * * $ components, will be described. The components will be reviewed with reference to Figures 5 and 6.

It will be appreciated that the selected components may form the basis of other aspects of the present invention. The present invention is not limited to combinations of items in the full list of components listed below. It will be apparent from the description that other aspects of the invention pertain to only a portion of the listed components, such as means for increasing the concentration of nitrogen and / or phosphorus and / or potassium; energy production based on the components of the extraction tank, lime digestion and roaching, as well as animal welfare and processing of wastewater.

Obviously, the following aspects, which are mainly related to disinfection, do not necessarily contain all the components that will be presented later. Obviously, the disinfection aspects include only a combination of some of the components listed below.

The animals shown in Figure 1 provide optimal conditions for food safety and food quality, animal welfare and working conditions for the farm workers, as well as for the treatment of slurry, and are suitable for use in the GfeanFarmEne / gy system, emissions, petrol ammonia, dust, odors, methane, nitrous oxide and other gases are minimized.

The facility consists of one or more early partitioning buildings with a total of 10 wards, capable of housing 250 animals per year, each ward | It houses 640 piglets weighing 7-30 kg or 320 slaughter pigs weighing 30-98 kg.

** * ΛΤΑ

It is estimated that approximately 10,000 m 'of sludge is formed each year. This comes with about 0000-10000 m ^{3 of} wastewater which is recycled to the plant. The following main conditions must be fulfilled for the plant:

1) Two-climatic system: Leads should preferably be designed to be dual-climatic. The rear end of the pens should be provided with a movable roof, which allows the pigs to be placed under a roof in a relatively warmer environment or in a relatively cooler environment elsewhere on the pen. The temperature difference should be 5-WC between the two parts.

When the piglets reach a weight of about 30 lbs, the roof should be adjusted to generally allow lower temperatures in the building so that the pigs can heat up below the covered area. By ensuring lower temperatures, it is also possible to increase air movement during cooler periods.

2) Where the animals live: The pigs are preferably fed a straw from a vending machine. In this way, we stimulate the searching and barking behavior, because you have to scrape the straw from the machine. Straw also serves as an energy source in the power plant.

3) Heating: heat from the power plant is preferably recycled to the animal beds. The heat can be provided by two independent circulating systems. One system is located under the roof and provides SÖ-SS ^ C, which creates a comfortable microclimate for pigs while keeping the land dry and reducing the growth of bacteria on it. The other system delivers heat through pipes placed along the walls of the building into the airspace of the building. The second circulating system also has controlled ventilation.

4> Showers: Showers are preferably located above the floor covering Ά of the total floor space. The pad encourages the pigs to place their feces on it and not on hard ground. The shower water washes the feces into the sewer, thus preventing the formation of odors and the evaporation of ammonia, etc. Pure, solid soil significantly reduces the risk of infections caused by pathogens, fertilizers, X & almononeia, Lavéonia _(< pffe.).

5} Rinse: We recommend flushing the channels several times a day. Rinsing is carried out with process water from the power plant. The manure is fed through a valve into a central channel,

6) Gutter Flush: The free surface of the fertilizer is reduced by using some kind of gutter while simultaneously rinsing the gutter optimally * 9. This is key to reducing odor emissions from livestock farms.

7, Ventilation: Ventilation is designed to provide maximum airflow

20% below the floor and the bottom of the pad, the central .X ventilation passageways between the double V-shaped channels should be provided. In 60-80% of the year, 20% of maximum ventilation provides sufficient airflow.

8) Feeding: Feed the feed with a wet feeder, which, if required, is sure to feed the feed.

In the following, the operation of the slurry collector 2 is described. The purpose of the slurry collector 2 is to collect the slurry generated during the daily cleaning of the central plant. The slurry collecting tank 2 acts as a temporary storage tank from which the slurry is pumped into a main receiving tank 3. The slurry is allowed to flow by gravity into the zagygyöjtő gyöjtőtartályba 2 _x 2 zagygyűjfő the collection container volume can be any suitable size. jyefdstdM 50 m ^a . The slurry collector 2 can be made of concrete and placed under the floor of the building, so that the slurry from the building can be led by gravity.

The slurry is preferably pumped from the slurry collector tank 2 to the main receiving tank 3, and other types of slurry or waste from other sites or plants can also be introduced into the main receiving tank 3. Examples of such fertilizers are slurry, cattle manure, molasses, vinasse, silo, etc. These materials are transported by car to the 3 main drum tanks and filled directly into the drum. The volume of the main compartment 3 may be of any suitable size, so that the overflow is 1000 rn ³ . The liquid color in the extraction tank is preferably controlled by a pump which pumps the slurry out of the main receiving tank 3. The dosing control can be manual or automatic. The maximum pumping capacity can be any appropriate value under the given conditions.

When the slurry is pumped from the main receiving tank 3 to the extraction tank, lime is added to the slurry to increase the pH. The lime feed line is preferably configured to add 30-80 g CaO to 1 kg of dry matter. The lime is preferably mixed as a powder in the slurry, which can be blown from the truck into the silo. The volume of the skier, the capacity of the skis and their food circles, is SO-TS m ³ . The amount of 30-88 g per kg of dry matter corresponds to an hourly | tofluorophenol ~ 12 kg * ·: «. * *

X «<* f * φφ'ΦΦ * * Μ φ * ♦ ♦ ♦>

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-37CaO, while 3.5 m ^{3 of} 6% solids slurry per hour is processed.

If lime is added directly to the slurry containing 6% solids, the amount of lime per kg of dry matter is 60 g of Wötefeel, ie 8.8 kg of Caö per hour. However, it is preferable to feed the lime directly into an alkaline, high-pressure sterilization and hydrolysis unit. When the lime is fed directly to the high pressure unit (E-media contains 20-70% solids), the lime dowel contains 30-60 g / kg of total solids. If 60 g of calcium oxide per kg of dry matter are added, 342 kg of calcium oxide are added to one portion of slurry, and 171 kg of kaldum oxide is added to one portion of slurry and 30 g of calcium oxide is added.

The balance 5 preferably measures the incoming E-media, i.e. the mass of the organic matter containing the energy. Sellers will conveniently determine the type of media -Petadium deep sleep or various energy crops that are shipped to the plants.

The specification must be specified by selecting the relevant E-media in a control panel. Based on the vendor information, the weight of the incoming E-media and their characteristics are recorded.

The control determines the following for each E medium (see alkaline hydrolysis);

«Energy content ♦ required heating time ♦ required rest time.

In the following, the operation of the 6 receiving stations that collect my deep and energy plants will be described. The 8 receiving stations collect litter from poultry or other animals and energy crops. This station is preferably a large silo equipped with a plurality of conveyor screws along the ground. The lorries of the E-media are discharged directly into the silo 7. The volume of the silo reservoir 7, ttetv <capacity, may be any suitable value under the given conditions, so that the Medium containing 51.5% solids of Medium is circulated annually | It can accommodate 9800 tons. The volume of the 7 silo tanks ranges from a few cubic meters to 100 uL, which corresponds to 3 days, more precisely 65 hours. The container material is preferably betpn / steel.

The 7 silo tanks for energy crops are used to store energy crops and are preferably preserved as silage fodder. The capacity / capacity of the silo 7 can be 5000-16000 m ^s . The silo 7 can be a closed storage tank where the silage effluent from the tank is collected and pumped for 3 persons.

The feeding and homogenizing system 8 for litter and energy plants is preferably received from the conveyors at the bottom of the main receiving container 3, and the E-media can be conveyed by further conveyor screws to the cooking units where it is preferably loosened by an integrated loosening device. The system volume / stubble tree may be any suitable value, which is 1.5 m ³ E-media / night, as required under the circumstances, Thus, including 8200 tons E-media / year, The capacity of the 8 transport and homogenization system is preferably at least 4 double | 30 minutes. The addition of E-media is controlled by three basic parameters, namely volume, density and time. Based on these three parameters, the volume processed per unit time, Time and thus the total volume and weight can be calculated.

Hereinafter, the operation of the 9 alkaline high pressure sterilization and hydrolysis units (hereinafter briefly; 9 high pressure lime cooking units) will be described. The 9 high pressure lime brewing units have two main functions, on the one hand. In e-media, especially from different poultry. and the hydrolysis of the structural components of the litter in order to make them suitable for use in 'mlkcb' 1 rotting tanks,

The 9 high-pressure lime digesters will preferably eliminate or at least significantly reduce the number of BSEprions when present in the in-plant waste, such as raw meat, bone meal, animal fat and similar products derived from the processing of non-animal animals. .

The high pressure lime brewing unit 9 is filled by the conveying and homogenizing system 8 with E-media types of the specified type at the time the balance is put into operation.

The high pressure lime brewing unit 9 comprises two identical components, namely two elongated tubular horizontal chambers having a central thread. The two tubular chambers are mounted on top of each other so that the lower chamber can be easily filled. The units are covered with a hollow jacket on their underside. The mantle transfers the heat of the steam below them to the E-media

The lime is introduced into the upper cooking unit from the 4 silicate vessels containing calcium oxide by introducing 342 kg of potassium oxide per portion.

The lower brew unit receives preheated E-media from the upper bracket.

Transfer the contents of the lower unit into a small 25 m ^s mixing tank. In this container, the E-media is mixed with the slurry from the main receiving tank 3 and the mixture is drained into the extraction container.

The calcium oxide inlet rain includes a permeable portion through which the calcium oxide can be filled directly into the mixing vessel located below the two tubular chambers. By mixing sterilized Media and crude slurry from the receiving tank in the mixing tank, a homogeneous biomass is produced while recycling the heat of the E-mediums.

The most important parameters of the process are as follows; dry matter content, temperature, pressure and pH of E-media, among the many possible combinations of parameter values, the optimal parameter set is as follows; 18 ° C, ⁸ x ^{10 5} Pa, Remidely 38% dry solids, batch buffer at pH 12.

The duration of treatment in the 9 high pressure lime brewing units consists of several periods, as follows; 1. Loading; time; 2. Preheat time in upper tube; 3, Heating time in the lower tube; 4. Rest time at specified temperature and pressure; 5. Pressure Relief Time; 8. Evacuation time; and TITLE 7 time.

The loading time is the time required to deliver the Emelums to the high pressure sterilizer and mix it with the added slurry. The loading time is 10 minutes from Ref. After loading, the Emédlumck must be heated to 18 ° C at a pressure of 8 x 1 ⁵ Pa. Preheating takes place in the upper tube, while normal heating in the lower tube. The heating time is expected to be | eOrötbeíü | 30-40 minutes.

The treatment time of the mixture at the desired temperature and pressure, i.e. 18 ° C and 6 x ^{10 5} Pa, takes approximately 40 minutes,

The pressure reduction time is approximately 10 minutes, the excess pressure is discharged into the extraction tank,

Evacuation is carried out with the help of a conveyor screw.

d- 3., * * ο «*«

.... 40 ....

C1P time is the duration of cleaning if needed, although this cleaning is usually not required.

The high pressure cooker has a volume of IU m ³ units and a filling rate of about 75-90%. The volume of the mixing tank is 25 m ³ .

The following table summarizes the most important treatment parameters,

value range Selected value Why Take dry content 10-30 30 crowd% Temperature 120-160 100 C Pressure 2-6 6 x10 ^s Pa pH 10-12 2 pH

In the vendor panel where the E-mediums are registered, it is advisable to define the following parameters for controlling the sterilization unit: Oy, Volume and type of Mediums. In this way, it is possible to determine the following for each E-media delivered to the high pressure cooker;

- the energy content of each E-medium

- required heating time

- treatment time required

- required mixing time for mixing with the slurry

- energy demand dependent on N-media

- charge rate, signal from radar / ml microwave sensors

- the empirical values observed by the operator.

Further, a mixing vessel 10 is provided for mixing the high pressure sterilized E-media and the crude slurry. After sterilization and hydrolysis in the high pressure unit, the biomass is allowed to expand in a mixing container 10, preferably located below the high pressure unit. The overpressure, i. E. The steam, is discharged into the mixing vessel W in order to pre-collect the ammonia and transfer the heat to the biomass in the extraction vessel before it expands in the mixing vessel 10.

The purpose of the mixing container 10 is to mix the cold, raw slurry from the receiving container and the hot, sterilized E-media to ensure that the two media are

♦ *** ν ♦ Ensure heat transfer between y and mixing of the two media. Heat transfer is heat recycling.

The volume of the mixing vessel 10, for example, has a capacity of about 26 m ^3. The material of the mixing vessel 10 can be any suitable material, for example insulated glass fiber. The operating temperature of the mixing vessel 10 is typically about 50 ° C to 50 ° C.

The biomass contained in the liquid biomass storage tank 11 must be used to provide sufficient biogas at the start of the whole mill. However, this is only applicable if liquid biomass is available. Examples of liquid biomass are fish oil and animal or vegetable fats. Vlnas and molasses can also be used, but their use is not recommended due to their relatively high water content and thus low potential energy content per kg of product.

The storage volume / capacity of the liquid biomass container 11 is typically about 50 m ³ The material of the container 11 is preferably stainless steel. The container 11 preferably contains liquids and solids having a particle size of up to 5 mm. For controlling the temperature, the tank 11 is preferably provided with a mixing and heating system. The tank 11 also includes pumps which convey the contents of the tank to the digestion tanks. The temperature in the reservoir 11 is preferably at least 75 ° C so that the oily or greasy biomass can be pumped into the digestion tanks,

The extraction and disinfection container (hereinafter briefly; extraction container 12) preferably receives the following materials;

- slurry from the 3 main bins and / or

- E-media from 9 high pressure lime brewing units and / or

optionally liquid biomass from the liquid biomass container 11 and / or

- waste water from decanting or possibly from potassium precipitationA-A ·

The extraction tank 12 serves to regenerate the heat used in the high pressure boiler by heating the slurry from the main receiving tank 3 and using this heat to mix the E-media with the slurry so that a homogeneous mass is passed to the digestion tanks and the pH is controlled. and further disinfecting the slurry prior to introduction into the digestion tanks.

The extraction and disinfection tank 12 is used to remove ammonia in a first step, and in the second step to recover the recovered gas to an absorption column which

- ♦ · **. » ϊ *** * ** * \ Φ <

*. Φ -Φ »is common to the absorption column used in the final subtraction process. Vaccine pathogens and slurries are prepared for anaerobic rotation.

A preferred embodiment of the extraction vessel 12 will now be described.

The bottom islands of the tank are provided with a concrete cone which is inclined downwards at an angle of 20 °. The sediment and sand are removed from the bottom of the tank with a mammoth pump. At the bottom of the container is placed a sand grinder which can be emptied through an external line. The tank can also be drained through the filter.

The top of the container has a tapered configuration consisting of sandwiched polyester (embedded bean) layers in a sandwich structure. The taper has an angle of about 10 '. A water sprinkler system is mounted on the top of the tank to eliminate overburdening during the mixing process and the general process. At the top of the cone is a slow-moving agitator system that provides optimum homogenization, optimum evaporation of ammonia, and optimum distribution of material in the material. Ammonia is passed through a tube containing wet air. absorbent unit.

The walls of the container, Wetvei, are formed as a cylinder consisting of sandwiched, insulated layers of isophthalate polyester (embedded foam). Inside the container ÍWofbelűt '600 m in length and ^4.5> ~ es heat pipes are arranged in ring formation for the purpose of heating media. Some temperature transmitters are also integrated to control the heating process. A pH meter is also included to control the amount of acids to be mixed with the medium. At the bottom of the reservoir is an insulated pumped pump chamber on the outside of the cylindrical wall. An ammonia vapor diffuser is located in the center of the tank. The ammonia vapor generated in the alkaline sterilization and hydrolysis unit is sprayed into the material in the container.

The cylindrical wall has a diameter of about 12 m and a height of 9 m. This means that the useful volume of the tank is about 1000 m ^and, including the lower cone as well.

The hydraulic settling time of the slurry and E-media is around 7 days, while the absolute minimum settling time is around 1 hour.

A preferred version of the extraction container 12 is made of concrete, reinforcing iron and pressure insulation insulation. The media contact surface is coated with isophthalate polyester to protect the concrete and reinforcing iron from corrosion. All pipes at the bottom of the tank are made of polyester or stainless steel. A ♦

· »*

The top and bottom of the container are essentially sandwiched, insulated with a layer of polyester (embedded foam). All tubes are made of either polyester or stainless steel.

The container also contains additional components. The mixing element is made of stainless steel while the heating elements are made of coated steel and / or stainless steel. All other components inside the tank are made of stainless steel,

Suitable parameters for the mixing of the ammonia recovered from the slurry include, for example, a temperature of about 70 ° C, a pH of about 10-12, a liquid-gas ratio of less than 1: 400, an operating time of 1 beta, greater than 90% efficiency,

The process parameter in the extraction tank 12 may include the following values, e.g.

media:

Operating Temperature·.

any organic fertilizers and pre-sterilized solid or liquid E-media, various liquid organic wastes, calcium oxide 0-8 ° C working gas composition: 80% NH ₄ , 15% CO ₃ , 3% Ö ₂ , 2% other gas thermal insulation k-value: 0.20 W / m ^s K maximum working pressure: + 2x10 ³ Pa abs, (no vacuum) maximum viscosity in media: 15% (TS) acidity: 5-10 pH particle content in media (sand): 1-2% maximum temperature in the heating elements: maximum heating elements

9O ° C

800 kW total rpm gear: 7.5 kW (20-28 rpm)

The extraction container 12 transfers the treated material intended for rupture to the rotting container. In a timed process, the material is passed into digestion tanks. Material demand depends on the digestion process in the digestion tanks. One, two, three or more digestion tanks may be used in the system.

b- ^J »»

-44-Α 12 extraction tanks are regularly filled with alkaline high pressure sludge and E-media. The aim is to prepare a material containing 15% solids. The amount of material in the tank is controlled by a few level switches. The amount of dry matter is controlled by a dry matter measuring unit. After loading the slurry and E-media, you can drain the Medium into digestion tanks every hour.

The extraction tank 12 is preferably vented with an ammonia-absorbing unit and the CaO requirement is controlled by a pH measuring unit,

The temperature of the E-media is controlled by means of a temperature transmitter.

During a timed process, water can be pumped optimally into the spray system to prevent foaming.

The digesters 13, 14, 15 used for biogas production will now be described.

The biomass is digested with a multi-stage digestion system, preferably consisting of three digestion tanks 13, 14, 15. However, the system may also contain fewer or more rattan containers.

The digesters 13, 14, 15 are preferably interconnected so that biogas production is as flexible and optimal as possible. The digestion tanks 13, 14, 15 are designed to be routinely operated both at the field temperature, i.e., 45-85 ° C, and in the field, i.e., 25-45 ° C,

The digestion process can be optimized for organic material feed rate, flushing time and maximum digestion (at least 90% by weight). The tanks may include spiral loops for heating the biomass to a convenient operating temperature.

A slow-moving agitator system fixed at the top of the tank allows for optimal homogenisation and optimal distribution of heat in the biomass,

The pH can be controlled by adding the right amount of organic acid (liquid),

The 13,14,15 digestion tanks preferably receive the following media:

- E-media from the 12 extraction tanks

- liquid biomass from the 12 extraction tanks holding the liquid biomass

acids from the acid reservoir 18.

-45Α 13, 14, 15 A talented embodiment of a rotting barrier preferably has the following structure:

At the bottom of the tank is an insulated concrete block with a side wall that slopes down at an angle of 20 °. The sediment, thinning sand from the bottom of the tank with a mammoth pump. At the bottom of the tank is a sand filter which can be emptied through an external pipe. It is also possible to empty the tank through the sand filter,

On the top of the tank is a cone made of mild steel. The taper has an incline of about 104. A water spraying system is provided on the top of the container to prevent foaming during the mixing process and the general process. The biogas is drained into the gas cylinder in a tube containing moist air.

The side wall of the digestion tank 13, 14, 15 is made of mild steel. Inside the tank there are 5/4 "heating pipes approximately 600 m long, ring-shaped to heat the media. The tank also includes temperature transmitters to control the heating process. A pH meter is placed in the tank to control the amount of acid added to the media. At the bottom of the reservoir, on the outside of the cylindrical wall, islands are provided with a valve pump chamber.

The volume / capacity of the digestion tank 13, 14,15 can be arbitrary, so that the net te

1700

The material of the digestion tank 13, 14,15 may be as follows:

The bottom of the tank is made of concrete, reinforcing iron and pressure-resistant insulation. The media contact surface is coated with isophthalate polyester for corrosion protection of the coating and the reinforcing iron. All tubes at the bottom of the tank are made of either polyester or stainless steel.

The top and sides of the tank are basically made of mild steel. Top and side pipes are made of polyester, stainless steel or mild steel.

Both the agitator and the heating elements are made of mild steel. All other components inside the tank are made of stainless steel or mild steel.

The process parameters in the digestion tank 13, 14, 15 may have the following values:

media:

any organic fertilizer, in particular pig manure, loose energy crops, operating temperature:

operating gas composition: k value of thermal insulation:

maximum working pressure maximum viscosity various organic wastes, CaO, organic acids.

35-58 ^; 'C

65% MoH «, 33% CÖ ₂ , 2% other gases. 0.25 W / m ² K, where heat loss is estimated to be 10 kW + 2x1 µ ³ Pa abs, (no vacuum) in media: 12% (TS) acidity: 5-10 pH abrasive grains in media (sand): 1 -2% maximum temperature in the heating elements: 8o ^; C fuel heater maximum power: 600 kW Power transmission speed: 7.5 kW (20-25 rpm).

The rothasztástfkőrüfbelöl be performed at 55 ~ ^C. The estimated heat loss is about 10 kW. The biomass in the tank can be heated to 5-5S * C for 14 days and, if necessary, acid can be added to the biomass to adjust the pH.

For adjusting the ρ érték value of the biomass in the digestion tanks 13,14, 15, the system preferably also includes an organic acid storage 16,

Following the digestion of the biomass in the digestion tank 13, 14,15, the biomass is pumped into a small buffer tank before being separated into different fractions in the centrifuge 18.

The decanter centrifuge 18 is used to extract solids and phosphorus suspended in biomass.

The decanting centrifuge 18 separates the digested biomass into two fractions: a fraction containing solids, especially phosphorus, and a fraction containing waste water.

The solid fraction contained 25-35% solids. <0.50% of solids and 65-80% of phosphorus are removed from the digested biomass. -99% can be obtained. The solid fraction is transported to the container 19 by means of a screwless conveyor.

Sludge water contains 0-1% dissolved solids and dissolved potassium. The amount of solids depends on the amount of PAX added. The most important component of wastewater is dissolved potassium, which represents 90% of the original potassium content in biomass. The wastewater is pumped into a 25 wastewater tank

The solids fraction, often referred to as the F fraction, is transferred from the 18 centrifuging centrifuges to the containers by means of conveyors and conveyors, which are known as "fractional centrifuges". They form a P-fraction transport system.

A common conveyor belt: transports the P-fraction to a container where it is accumulated, covered with a layer of compost and allowed to compost. Composting further dries the P fraction, reducing the dry matter content to 5080%,

It is advisable to effectively remove the ammonia from the waste water and reduce the amount of ΙΜΗλ-Ν to about 10 mg / l or less.

The second ammonia deprotection step is preferably carried out with a dipper 20 operating at ambient pressure. Extraction of ammonia is most effective at temperatures between 180 * 0. A critical operating parameter is the amount of energy used to heat the introduced material. Therefore, with the help of the purification column 20, the introduced material must be preheated to about 10 ° C prior to introduction into the ammonia absorption unit 21. This is achieved by steam from a motor generator in a steam-water heat exchanger, possibly by a mixture of hot water and steam.

During heating, the feed material enters and passes through the ammonia absorption unit 21 while heating to the operating temperature by free-flowing steam in the opposite direction. The gas / vapor ammonia mixtures are next precipitated in a two-stage condenser.

From the bottom of the ammonia absorption unit 21, the ammonia-free water is pumped to a level controlled by an outlet pump.

The extracted ammonia is fed to the bottom of a two-stage purification condenser, where the ammonia gas is precipitated into a cooled ammonia condensate flowing in the opposite direction. The non-precipitated ammonia gas is the opposite in a further step

It is condensed in 48-directional clear water, which may be derived from the final reverse osmosis filtration step. If the use of an acid is desirable or necessary, sulfuric acid is preferred in this step. This makes it possible to produce higher concentrations of ammonia. The purification capacitor is preferably made from a polymer to allow the use of acids.

The construction of an ammonia absorption unit 21 for a first and / or second nitrogen removal device will now be described.

A precipitation purification device is used for the flexible use of the acids. The ammonia absorption unit 21 is preferably divided into two sections such that the non-condensed ammonia fraction in the first section condenses in the second section. This is done in a completely opposite direction, so that the amount of added water is reduced as much as possible. This results in a maximum ammonia concentration in the final condensate of greater than 2S%. The ammonia product can be pumped out by means of a separate pump or discharged through a valve on a circulating pump. Absorption can be facilitated by adding sulfuric acid to water flowing in the opposite direction.

The sulfuric acid used in the nitrogen removal process is stored in an acid storage tank 22.

The recovered nitrogen is stored in a container 23.

It is also desirable to use a gas container 24 as a buffer vessel from which the material is introduced, for example, into an engine generator.

Preferably, the waste water from the decanter centrifuge 18 is pumped into a waste water tank 25.

The waste water tank 25 is provided with a static-operated submersible microfilter. The purpose of the microfilter is to remove particles larger than 0.01-0.1 µm. On both sides of the diaphragm, a pressure difference of 2-8 x ^{10 4} Pa develops. In this way, the liquid flows through the membrane while the particles are retained by the membrane surface. To prevent scale build-up of the membrane, deposits on the membrane surface must be regularly removed.

The permeate extraction and membrane purification process is automatically controlled by a microprocessor control device. The extraction is periodically interrupted by a purge for a period of 35 seconds during a stopping time of 300 seconds. In this way, the total flow rate is 2-8 m'Y hours.

♦ ♦

... 49

Micro cracking. Ventilation may be used to assist. Ventilation generates shear stress on the membrane surface, which reduces limescale formation. Ventilation also ventilates the wastewater and also stimulates aerobic degradation of residual organic matter, nitration and denitrification. Any remaining odors, nitrates, etc. may be removed during microfiltration.

The permeate patter formed in the tank can be used for the following purposes;

- Windows, Stables, Ducts, Roofing Plates, etc. Wash.

- Further separation. The concentration of dissolved potassium can be increased by reverse osmosis, where the potassium fraction is stored in a separate container 26. The water used to wash the stables and stables can also be drained from this permeate stream,

Potassium can also be concentrated by other means, such as mechanical or steam compression. The method of compaction depends on the particular plants and the amount of excess heat available to the heat-driven compressor.

The waste water tank 25 containing the concentrate resulting from microfiltration must be emptied at regular intervals to remove particulate matter. The removed particle concentrate may be added to the K fraction or to the F fraction from the centrifuge of the decanter 18.

There are 28 separate containers for storing potassium concentrate.

The biogas produced in the rotary tanks 13, 14, 15 may contain traces of hydrogen sulphide (H ₂ S) which must be removed before the biogas is burned in a combined heat and power plant.

The gas must be purified by taking advantage of the ability of certain aerobic bacteria to oxidize K ₂ S to sulfate. For this purpose we use primarily the Thiobacillus strain which is well known in many terrestrial and marine environments. Other bacteria can also be used. so

For example, Thimlcrosplra or Suifolobus.

In order to keep the packaging material wet, a glass fiber container with a large surface area surrounded by plastic tubes must be flushed with impure water. The biogas is discharged through the filled column and an air stream, preferably ambient air, is added to the biogas stream. The purpose of adding ambient air is to adjust the concentration of oxygen in the gas to 0.2%, which is sufficient to oxidize H _to S, so that no biogas and oxygen is blown. A circular side blower is used to inflate the air.

The main component of the combined generating and electric power plant 28 (or gas engine 28 in short) may be a gas-powered rotor connected to a generator to generate electricity. The primary purpose of the electric and electric power plant 28 (fefflSsh§iT'f>) is to generate as much electrical energy as possible from the amount of heat available. The engine is preferably cooled by a water cooling circuit in which the water temperature is preferably 90 ° C and the heat used in processes, as well as for heating sheds and stables.

The extracted gas is used in a recuperator to produce steam. The steam is used as a heat source in the powerlift process, i.e. in the high pressure lime cooking unit 9 and in the second leaching column 20 of the digestion unit. Depending on the amount of steam, it is also possible to increase the concentration of potassium in the waste water

There is a heat exchanger between the steam and heat circuits, thereby allowing heat to be transferred from the gas transport system to the heat transfer system.

In addition to the above items, we also operate a steam boiler _; too. The gas boiler is used to generate the heat needed to start the process and can also be used as a backup power source for the system.

If the power plant were to produce more heat than needed, the excess heat could be evaporated in a chiller.

To start the power plant process by heating the digestion tanks 13, 14, 15, the heat is provided by an oil-fired boiler. As soon as the gas formation has started, the oil-fired burner is switched to gas-fired. As soon as the gas production is sufficient to start the engine, the engine will take over the heat generation.

In the following, the separation of potassium is described. There are at least two possible ways to remove potassium from wastewater. At relatively high levels of biogas production, the ntotor generator produces excess heat, preferably 16 ° C, that can be used to increase potassium concentration. Nutrient-free distilled water can be used for irrigation, recycled at the power plant,

At relatively lower levels of biogas production, a microscopic filter may be used to remove particles larger than 0.01-0.1 pm from wastewater, making the permeate suitable for treatment with a conventional reverse osmosis filter. The potassium concentration should be adjusted to 10-20%.

* · "

- 51 _

The second aspect of the process of the invention is in organic fertilizers, feed, slaughterhouse waste, meat and oste meal, pte. Significantly reduce and / or completely destroy BSE prions. This is achieved by a combination of pretreatment and rot. The components required for this, as mentioned above, are provided with a device suitable for pretreating the material containing the SSE prions. One such device is a high pressure lime brewing unit. The lime brewing unit can be used with various organic materials, hydrolysis of materials containing prions.

BSE prions are proteins that are resistant to attack by protein-degrading enzymes. If the temperature is preferably prions 140-18CPC, 4-8x1Q ⁵ psi and 10-12 bémlfeeBlj pH of from! the microorganisms are present in the bioreactors of the Vari and and since the ammonia has already been removed from the material, the total amount of nitrogen has been reduced. microorganisms are capable of producing additional extracellular proteinases and proteases which are capable of bridging BSE prions, and long treatment times also contribute to the efficient decomposition of BSE prions.

The third aspect of the process according to the invention is the removal of nutrients in the organic fertilizer, in particular nitrogen and phosphorus, and the refinement of the nutrients into commercial or "organic" grade fertilizers. This is achieved by combining the first aspect of the process of the invention with the use of a decanter centrifuge,

Nitrogen and phosphorus are the main nutrients in the sludge, which usually becomes redundant in the pellets. Nitrogen according to the first aspect! Extract and collect phosphorus in the digested slurry as described in process. Conversely, by treating the slurry in a decanter centrifuge, the phosphorus can be removed from the slurry along with organic and inorganic solids.

Thus, more than 90% of the nitrogen and phosphorus in the slurry is suitably collected in separate fractions. The remaining waste water contains a certain amount of potassium and traces of nitrogen and phosphorus. The wastewater thus becomes suitable for application to arable land at any time of the year.

♦ *

** »* ♦

- 52 Extraction of potassium from wastewater can be accomplished by additional attached membrane ventilation and filtration. In short, this means that a filter unit 29 containing a ceramic microfilter is used as both a diffuser and a filter. The filter unit 29 is immersed in waste water and operated with intermittent ventilation and filtration periods. Ventilation decomposes residual organic matter and creates inorganic flakes. The treated water on such a mat becomes suitable for membrane filtration, since scale formation is eliminated. Ventilation of the same membranes, namely counter-flushing with air, also prevents the formation of limescale.

The product thus produced is a concentrate containing potassium of potash and filtered water suitable for irrigation of soils where only a very limited area is required.

As in the first aspect of the process of the invention, the waste water can also be recycled to the sheds and stables.

The phosphorus fraction is suitable for further drying to produce commercial grade granules. The nitrogen and potassium fractions are of similar commercial quality.

In particular, the third aspect of the process of the present invention is to concentrate the major nutrients in the sludge and other organic matter, particularly nitrogen and phosphorus, and potassium into commercial grade fertilizers.

Combining the use of decanting centrifuges with other elements of the GFE biogas production and sludge separation system, in particular the NF extraction unit, may be particularly valuable to the farmers. Combining the nitrogen removal unit and the decanting centrifuges means that most of the nitrogen and phosphorus in the slurry can be separated and collected in two separate fractions. It is important to ensure that when phosphorus is present in the form of flakes, the phosphorus can be extracted with a decanter centrifuge.

Nutrients can be used according to specific needs, so they can be sprinkled on the ground. The wastewater generated behind the decanting centrifuge can be recycled through the pet stumps, the wastewater can be used to clean the floors and roofs of the stables, and has the additional benefits of good indoor climate, reduced ammonia and other gas emissions, regular rinsing of sewers, etc.

* * ♦ 9 · - * «»

- 53 The waste water. it contains predominantly potassium and, to a lesser extent, phosphorus. This means that in a process where ammonia is removed from the slurry and phosphorus is removed, nitrogen and phosphorus can be stored and used according to specific needs, while the wastewater can be treated as sewage throughout the year.

We estimate that the area to be fertilized is around (% of the total area to be treated with sludge, so that the total area available can be fertilized over a 4-year period with the available biomass.

Regardless of the possibility of further treatment of wastewater, many hosts would certainly be extremely satisfied with nitrogen and phosphorus extraction, even with the use of a single reactor for slurry digestion. Even with decanting centrifuge recovery can be omitted because by concentrating nitrogen, it produces a nitrogen-free slurry that can be applied to land at any time of the year, except during frosty periods.

It is highly advantageous that some parts of the entire system may be offered to a group of farmers, while to other farmers a combination of parts of the system may be appropriate. In all cases, nitrogen removal is what makes the use of decanting centrifuges important to farmers in practice.

The waste water from the entire process can undergo a final treatment according to market needs.

A major challenge is to treat wastewater to make it suitable for membrane filtration and to reduce it by more than 5% to 8%. Another challenge is the use of well-known, inexpensive and robust technologies according to a new principle.

Slurry ventilation is a well-known method, where ventilation in the ambient air for 2-4 weeks accomplishes aerobic digestion,

Ventilation provides the following results:

1, The remaining ammonia can be extracted and collected in an absorption column, which is preferably the same as that used during pre-treatment, i. during low temperature extraction (at 250 ° C). This requires a higher liquid to gas ratio, preferably about 1: 2000 (Uao et al. 1995).

2. The remaining organic matter and odorous components are decomposed (Camarero et al. 1998; Borion et al. 1998; Doyle and Noüe 1987; Garraway 1982; Glnnlvan 1983; Blouin et al.). 1988).

φφ φ

-543. Any ammonia remaining after the removal of ammonia is converted to nitrate (Argaman Y. 1984; Gönenc and Harremoés 1986),

Ventilation can be combined with filtration and a new waste water treatment technology combining microfiltration with ventilation and filtration with ceramic filters (Bouhabía et al. 1998; Scott et al 1998;

Zaioum et al. 1998; Engethardt et al. 1998). Energy efficient ventilation and filtration can be achieved in a single operation Ventilation can also be used to clean ceramic membranes by back flushing with air (Visvanathan et al. 1997; Silva et al. 2900).

In this way, an aqueous phase is formed which is very suitable for separation via a conventional osmotic membrane, if necessary, since the problems of descaling are minimal. Therefore, it is assumed that a greater amount of reduction can be achieved using substantially less energy, although a certain amount of energy can be mimicked.

even when membrane filtration is not used, ventilation may be motivated by the final removal of ammonia and removal of residual odor components.

The major devices of the fourth aspect of the present invention consist of pre-treatment units which are the following, an extraction tank, a high-pressure lime digestion unit, flexible and multi-stage bioreactors with at least 3 stages.

According to a fourth aspect of the invention, a large amount of biogas can be produced from a variety of organic materials, such as various organic fertilizers, energy crops, plant residues, and other organic wastes.

The pretreatment devices mentioned in the first and second aspects allow the use of a wide variety of organic materials, while the multistage biogas plant allows for the complete rotting of the material and thus the greatest possible amount of energy.

Nitrogen-rich and difficult-to-handle materials such as poultry manure and litter are pretreated in a lime-grinder. The cooked material is pre-crushed in a mesephile reactor before being introduced into the extraction tank and further reactors.

Pre-digestion ensures that organic matter in the slurry is decomposed and nitrogen is released in the form of ammonia, which is introduced into a solution. Thus, much of the nitrogen is collected in the extraction tank and * φ · difficult-to-handle organic materials are decomposed in further reactors at this power plant. Depending on the quality of the starting material, it is also possible to introduce it directly into the digestion tank before digestion in the reactors.

As a result, a large amount of biogas can be produced, that is, 5-10 times more energy can be produced than the sludge contains.

Treatment with GFE in a biogas production and separation system also ensures that nutrients return to farmland. The energy plants are digested in a separate reactor and the digested biomass is discharged into the extraction tank. Fibers that have not decomposed during the separation in a separate reactor are hydrolyzed in the same vessel and collected in the form of an ammoniacal nitrogen fraction. Nitrogen in energy crops can then be recycled to the soil and used to grow energy crops. About 1 to 3 kg of nitrogen can be recycled per ton of silo.

It is expedient to remove ammonia from the grain material according to the invention, which would especially prevent the formation of biogas at thermophilic temperatures (Hansen et al. 1993; Kryíova el al 1997; Kayhanlan 1994}.).

The process may conveniently be divided into a fermophile and a field (Dogba and 2hang 1999, Han et al. 1997; Gosh et al. 1985; Coierier et al. 1933). This division results in, among other things, increased energy production and operational stability, since biomass spends more time in bioreactors, which gives enough time for the methane-producing bacteria to decompose the materials. It is important to note that heating requires more power and a larger reactor size.

In addition to the above-mentioned two-step process, a reactor may be used in the plant for the digestion of slurry and other similar nitrogen-containing biomasses. Energy plants must also be shelled in such a reactor before being sent for further processing at the power plant. During pre-digestion, much of the available organic matter decomposes and forms nitrogen in the form of ammonia. The nitrogen can then be recovered in the extraction tank and collected in a nitrogen fraction,

Dried beet, maize, alfalfa, etc. contains about 1 kg of nitrogen per tonne, so it is important that the nitrogen is collected in the nitrogen fraction. Poultry manure contains even more nitrogen and can also be pre-digested before further digestion in the main biogas plant.

Ammonia extraction and hydrolysis also ensure that difficult-to-treat fibers become suitable for digestion as described in the pretreatment. The digestion described below ensures maximum gas production at the main biogas plant.

A fifth aspect of the system of the present invention is to maintain an optimal level of animal welfare and health when the animals are housed in pens and stables, and at the same time reduce the emission of dust and gases, such as ammonia. This is what we do. that the wastewater is passed through the shed for cleaning and rinsing of stables, floors, roofs, drains and thus recycled into the system. This will reduce the size of the surface which can release odorous substances, ammonia and dust into the interior airspace.

The system also allows the use of straw without increasing the amount of dust and ammonia emitted. Straw is an essential component of animal welfare, especially for pigs, but also for other animals. Straw provides material for animals to hike and lay down and on the other hand serves as a structural feed.

After treatment with a decanter centrifuge or possibly before the first digestion step, the effluent water is extremely suitable for cleaning the stables. Such rinsing with water removes the mixture of straw and manure from the pens, Stables.

Other embodiments of the system of the invention may be accomplished by combining various aspects of the invention. The first aspect of the invention is suitably embodied in each combination.

Accordingly, from the foregoing descriptions of the preferred aspects, it is obvious that the process in which

(I) removing nitrogen from the organic material, such as organic fertilizer and slurry, in the form of ammonia and, if necessary, controlling the organic material, (ii) feeding the organic material thus obtained into a biogas-producing rotting container, and (ii) digesting the organic material. producing biogas.

The above process also comprises the step of: step, with a decanting centrifuge, the biogas-producing digester!

The solids from * 57 * are separated to give separated phosphorus and / or potassium fractions, which are conveniently prepared in granular form.

One embodiment of the aforesaid process also comprises the step of returning the biogas digestion fluids to the stables or sheds, if necessary after a further purification step.

In another embodiment of the process of the present invention, a step of carrying out thermal hydrolysis and / or alkaline hydrolysis is carried out simultaneously with or subsequent to the recovery of the ammonia, wherein one or both of the steps mentioned above at elevated temperature and / or elevated pressure. execute.

The above-mentioned preferred embodiments of the process according to the invention, on the one hand, solve the problem of undesirable microbes. cause environmental problems due to organisms. Examples of microbes are Saimonella Typhimurium D7104 bacteria and / or BSE prions present in organic matter, such as organic fertilizers and their slurries,

A further preferred embodiment of the process of the present invention also solves the problems associated with meeting hygiene standards in barns or pens which are undesirable microbial organisms and / or BSE prions present in organic matter, mineral fertilizers and their slurries. reduction and / or total destruction.

Another embodiment of the process of the present invention also solves the problems associated with the additional use of expensive water in Stables and pens. This problem is solved by recycling the wastewater generated during the separation by decanting centrifuge used to separate solid and liquid materials. The dry. and liquid materials derived from the pretreatment of organic materials and / or the extraction of nitrogen, ammonia and / or anaerobic rotation leading to biogas formation. At the same time, it is possible to reduce the number of microorganisms in the waste water and / or to eliminate their presence by further purification steps.

The invention makes it possible to produce cheap fertilizers of commercially acceptable quality. This, on the one hand, with the removal of nitrogen inside it »»

This is achieved by extraction of 58 ammonia and separation of the phosphorus-containing granules and the potassium-containing granules by decanting centrifugation, which is carried out after a pre-treatment, preferably after thermal alkali hydrolysis.

Another aspect of the invention is achieved by the implementation of a process

ΆΎ which reduces the number of viable microorganisms (organisms and / or BSE \ i ·· prions) in the organic material.

i) collecting organic matter containing solid and / or liquid parts:

il5 is performed on the organic material. the following steps;

a) the organic material is hydrolyzed by high pressure lime at a temperature between 10 ° C and 22 ° C, whereby the lime is calcium hydroxide and / or calcium oxide and then

b) extracting the ammonia from the organic material treated with high pressure lime;

wherein the lime added to recover the ammonia and disinfect the organic matter precipitates the dissolved orthophosphates;

18) preparing processed organic material containing reduced amounts of viable microbial hormone and / or prion; and spilling the processed organic material into a biogas producing digestion tank, where the processed organic material is trapped, thereby producing biogas.

The process of the present invention eliminates the presence of a variety of microbial organisms, including, but not limited to, the following microbial organisms (organisms: animal T., '', '' Microbial organisms, infectious microorganisms, parasitic pathogen microbes and organisms). combinations thereof Microbial organisms include, but are not limited to, bacteria, vectors Camgylobacter, Saimonella, Yerslnia, Ascarls, and similar microbial parasitic organisms, as well as viruses, virulent substances and the like.

The liming step also serves to sterilize the organic material, as long as viable microbial organisms do not survive this processing step. Preferably, the lime is CaO or Ca (OH} ₂ , or substantially all of them. In the sterilization process, all other BSE prions and other phones present in the organic material are also preferably decomposed or destroyed. the number of microbial organisms and / or prions is reduced, the rate of reduction is 90%, 80%, 70%, 80%, but preferably at least 50%.

In a preferred embodiment of the process according to the invention, the biogas production can be enhanced by treating the organic material with high pressure lime before removing the nitrogen, however, organic material treated with high pressure lime can also be rot before the nitrogen cloning is carried out.

If the organic material is of vegetable origin, it is advisable to silage it before draining it for nitrogen removal. Plant-derived silage organic matter can also be rotted before nitrogen removal. The organic material to be harvested is preferably a perennial fodder plant, such as sugar beet, maize, alfalfa, and where appropriate, the vegetable greens processed.

The organic material is subjected to high pressure lime cooking at 100-250 ° C, 2-20 x ^{10 5} Wood pressure, and sufficient amount of lime is added to the material to maintain a pH of between 9 and 12. The operating time is at least 1 minute, but preferably at least about 5 minutes.

Preferably, the amount of lime added is from 2 to 80 g per kg of dry matter, from 5 to 80 g per kg of dry matter, from 5 to 80 g per kg of dry matter per 10 g of dry matter per kg of dry matter. , 15-80 g per 1 kg of dry matter, MrófbátSIt'20 * 80 g per 1 kg of dry matter, Iwrafb'40 and 40-80 g per 1 kg of dry matter | Per kg of dry matter.

The high pressure lime cooking unit can be operated with the following operating parameters; Wütbelő | A temperature of 120-22 ° C, ^a pressure of 2x10 sPa and preferably not more than 1.8 x 10 ^~ Pa, and at least 1 minute and preferably max. 30 minutes treatment time.

A further possible example of operating parameters is the following temperature of the brewer: 18 ° to 20 ° C, hardness of 1x10® Pa and preferably up to 1.6x10® Fa, pH 10-12 and treatment time of 5-10 minutes. .

The above process can be followed by a number of further steps. In one embodiment of the inventive method of the invention, the process is carried out by feeding the processed organic material into a biogas producing digester, digesting the processed organic material and producing biogas. One more

60 a possible step is the supply of agricultural land with processed organic matter to the outside environment, JpéidáetH. The external environment, examples! agricultural areas may also be supplied with residues from the digestion of processed organic matter. vas-ÁzrnK J

A further possible step is the removal of nitrogen and ammonia from the organic material prior to feeding the organic material to a biogas-producing digester. This solution results in higher and stable biogas production than before. The process allows for nitrogen; utilization of rich biomass after extraction of the nitrogen and subsequent digestion of the biomass in the digestate tank. The biogas is produced by digesting organic material partially decontaminated with nitrogen, ammonia.

The recovered nitrogen or ammonia is specifically absorbed in a column before being stored in a tank. Upon absorption in the column, the extracted nitrogen, Htetvaf abimonia, is absorbed into a column containing water and an acidic solution, preferably sulfuric acid, before being stored in a container.

A possible embodiment of the process according to the invention comprises the following steps; (I) inactivating the viable microbial organisms in the organic material and / or partially or completely destroying them by (a) treating the organic material with high pressure lime and / or (b) heating the organic material to a predetermined temperature and / or subjecting it to a predetermined pressure and / or adding a base or an acid to the organic material and (c) at least partially hydrolyzing the organic material; wherein steps (a), (b) and (c) are performed simultaneously or in any order sequentially; and (iii) extracting the nitrogen from the processed organic material, triturating ^; - a quantity of ammonia; (l) feeding the nitrogen-free particulate material to a biogas producing digestion tank; (arc) digesting the non-nitrogen-free organic material; and (v) providing digested organic material containing biogas and at least a reduced amount of viable microbial organism and / or BSE prion.

It is highly advantageous that the organic matter obtained by rot is substantially free of BSE prions /

The extraction of the nitrogen, this amroma, is conveniently accomplished by initially adding a specified amount of lime to the organic matter, which is sufficient to raise the pH above 9, preferably above 40 ° C, or to raise the pH above 10 preferably above 4 ° C * ♦

.... 61 ·········································· temperature temperature · · · · · · · · · · · · · · · · · · · ·

The invention in this embodiment, the temperature is preferably 50 ° Cν Ά '> · higher than, ^s spétáátá.55 C ná? L higher Hftó ^ SO ^ C higher.

In one possible process, the treatment time is 2-15 days, fpd <4 ~ 10 days, walking time 6 ~ 8 days, and the process parameters can be as follows: pH 8-12, temperature 70-80 ° C, the liquid to gas ratio is less than 1: 400 and the treatment time is about 7 days. Alkaline conditions can be provided by the addition of any base. However, it is advisable to raise the pH by adding CaO or Ca (OHb,

The organic material may include solid and / or liquid parts such as various organic fertilizers and their slurries, vegetable residues, ski slides, animal carcasses or parts thereof, slaughterhouse waste, meat and offal,

50% solid up to 30% solid in any combination. The organic matter is the same

containing up to 40% solids, up to 20% solids. The organic material may also be in liquid form, in which case it may contain up to 10% solids.

The organic material may further comprise straw, fibers or sawdust, so that the organic material may contain a large amount of fiber, preferably in a proportion of more than 10% w / w. The organic material may also contain high amounts of complex carbohydrates, including cellulose and / or hemicellulose and / or lignin, preferably in amounts greater than 10% w / w. In the organic material containing cellulose for high pressure leaching, cellulose decomposes into small organic acids, acetic acid, acetic acid, lactic acid, etc.

The organic material may contain deep litter or organic fertilizers, in particular cow manure, pig manure or poultry manure. In addition, they may also use animal organic matter, such as dead animals or parts thereof, slaughterhouse waste, meat and bone meal, blood plasma or any other animal product which may be hazardous due to the presence of BSEprlons or other protons.

The organic material contains solids or essentially only solids less than 10 cm in length, such as less than 5 cm in length, and less than 1 cm in size.

* ¢:

♦ »χ

V <A ♦ * X χ «**

Preferably, the organic material is loosened prior to treatment in the high pressure lime grinder, preferably by means of a conveyor with a loosening device, preferably made of stainless and acid-proof steel. The conveyor feeds the organic matter to the limestone, where the organic material is conveniently heated by injection of steam or steam in the chamber around the lime digester, if any combination.

The particulate material may contain proteins or similar organic molecules containing elements, such as amylic acids or combinations thereof, that form BSE prions or other prions, wherein the BSE prions or other prions are eliminated, directly destroyed, or subjected to high pressure destruction. with limestone steam and / or with additional roasting, • anaerobic digestion of carob. The organic material of animal origin preferably contains a large amount of nitrogen, preferably greater than 10% nitrogen.

The organic material produced in the form of a liquid slurry is formed by adding water and / or a small amount of organic material, preferably less than 10% solids in water. The added water may be recycled water, water containing low concentrations of silage grains, and / or water collected after purification of stables and / or animals and / or water obtained by digestion prior to the nitrogen removal process and / or water obtained from one or more biogas plants , and / or water obtained by concentrating phosphorous fertilizers and / or water obtained by concentrating potassium fertilizers, and / or

In a preferred embodiment of the process according to the invention, waste water from the water production plant, effluent from the concentration of phosphorus fertilizers, water from the concentration of potassium fertilizers or collected rainwater.

In a preferred embodiment of the process according to the invention, a minor portion or a large portion of the urea and / or uric acid in the organic material is converted to ammonia and the. ammonia is collected, if necessary, after absorption in an absorption column as described above.

In addition to high pressure lime digestion, field and / or productive digestion can also be carried out. digestion plant before or after the nitrogen has been removed from the organic material,

In all cases, rotting is carried out with a bacterial population capable of rotting in the field or through fruit. Anaerobic digestion is one possible method of digestion.

digestion is preferably about 15 and preferably at most 55 körtébe® üh2S ^S C * C and preferably up Aöföfeetöi 'between O5 ° C, under -p, Peled desrefbek ^ -S and is preferably carried out up to between 45 ° C.

The digestion is preferably carried out for a period of 5 days and preferably for a maximum of 15 days, for a period of from 5 to 10 days.

In one embodiment of the process of the invention, biogas production is carried out in one or more plants with microbial organisms, preferably a bacterial population, and the organic material is digested anaerobically. Preferably, the bacteria produce mainly methane and to a lesser extent carbon dioxide during the rotting of organic matter. Biogas production can be carried out in one or more plants, preferably by bacterial digestion of the organic matter by anaerobic digestion.

In one embodiment of the process according to the invention, the biogas production process is carried out in two plants, whereby the grain material is anaerobic bacteria, and first in the first plant is digested with bacteria, then the organic material treated with lermophilic digestion is transferred to the second plant. additional digestion with bacteria.

The temperature at which the fruit's rotting reaction is preferably 45-75 ° C,

60 ^c C.

The mesofl! During the reaction reakciéhőmérséklei preferably 20-45 ^c C.

^S 35 C, A fruiting reaction, as well as the field of reaction, preferably S ~ 15 days pétdáuk is carried out for 7-10 days.

Any foam formation may be reduced by the addition of polymers and / or vegetable oils and / or one or more salts which are preferably rapeseed oil. The salt may be calcium oxide and / or calcium hydroxide.

In biogas production, the desired flocculation of materials and particles is burned by the addition of calcium ions, which are capable of forming calcium bridges between organic substances and inorganic substances in solution or suspension, since calcite bridges cause the flocculation of the particles. Addition of calcium ions> f * «♦ *« • 'Φ φ also causes precipitation of orthophosphates, petroleum-derived PO4 ³ ' ions. Phosphate ions are preferably precipitated in the form of calcium phosphate Ca ₃ (PO ₄ ) ₂ and precipitated calcium phosphate is preferably suspended in the slurry.

The biogas produced can be delivered to a gas engine suitable for generating heat and / or electricity. The abundance may be used to heat high pressure lime and / or digestion tank and / or digestion reactor and / or one or more biogas plants and / or animal and / or human homes and / or to heat domestic or domestic water. Electricity can be transported and sold for distribution in the power grid. In a preferred embodiment of the process of the invention, the remaining, nitrogen-free, sterilized and decomposed organic material is sprayed onto the arable land.

In addition to (fi) reducing and / or eliminating unwanted microbial organisms, (ii) increasing biogas production, and (ii) providing highly utilizable, non-nitrogen-free, sterilized, and digested organic material, in its variant, the organic matter is prepared from nitrogenous fertilizers by (a) collecting, in a nitrogen-free step, the nitrogen extracted from the organic matter, kiewe apple tree; (b) absorbing the collected potassium N, N, ammonia in water or in an acidic solution, preferably in a solution containing sulfuric acid; and (c) producing nitrogenous fertilizers that can be applied to arable land,

Another embodiment of the process of the present invention is for the production of phosphorus-containing fertilizer from an organic material containing a source of phosphorus. In the process (1) the slurry is discharged from a biogas producing digestion tank into a separator, (II) separating the digested organic and inorganic material into a solid and mainly liquid fraction, and then (III) preparing a mainly solid fraction containing partially phosphorus, preferably calcium phosphate in the form of Ca ₃ (RO .. <) 2, and where the grain phosphates are suspended in the slurry, the organic fraction thus produced is suitable for use as fertilizer containing phosphorus on suitable agricultural land.

The separator for separating the digested organic material and the inorganic material into a solid and mainly liquid fraction is preferably a decanter centrifuge. The substantially solid fraction containing phosphorus may be dried if necessary and granulated with * * ~ 6S ~ phosphorus containing fertilizer by allowing the Pfraction to be composted under an air-permeable sheet or lid,

The effluent water from the biogas production and the water remaining after the separation of the solid components can be conveniently reused for the digestion of the silo and / or high pressure lime and / or in the nitrogen extraction process and / or in the biogas plant and / or for cleaning the stables. and / or for irrigation of arable land and / or water can be discharged to a conventional sewage treatment plant.

The invention also relates to a process for the production of substantially pure waste water. In the process, a liquid fraction is produced with a separator, preferably a decanter centrifuge, in an extremely small amount, preferably 5% w / v, e.g. up to 1% w / v, e.g. up to 0.5% nW, up to 0.01% w Contains / V of waste water containing nitrogen and phosphorus, The liquid phase essentially does not contain sources that allow the production of zoonotic viruses, infectious bacteria, parasites or other infectious agents such as BSE phones or other prions. In some embodiments of the process of the invention, it is acceptable for the waste water to contain up to 10% of the nitrogen and phosphorus originally present in the slurry,

The present invention also relates to a process for preparing potassium-containing fertilizers from an organic material containing a potassium source. In the process (I), the liquid fraction formed in the first separation step is led to a second separation step, wherein the first separation step separates the phosphorus organic materials, (ii) separates the remaining organic and inorganic mixture from the liquid, and (ii) a potassium-containing solid fraction, which solid fraction can be used as a potassium-containing fertilizer that can be applied to suitable fields.

In the second separation step, the potassium-containing fraction is preferably passed through a ceramic microfilter, which is ventilated batchwise and which filters the waste water. By venting, the remaining organic material is decomposed and inorganic flakes are formed.

The present invention relates to a process for producing pure wastewater, wherein the wastewater is treated in an aerobic system suitable for reducing and / or completely removing the nitrogen and phosphorus present in the water, and which conveniently decomposes the remaining organic matter and odors. components, thereby producing wastewater that is substantially free of nitrogen and phosphorus. The waste water thus obtained is suitable for irrigation of suitable arable land or recycled through animal farms.

The aforementioned ventilation can be carried out in ambient air over a period of 2-4 weeks at a temperature of 20 ° C and a liquid to gas ratio of about 2000; The extracted nitrogen can be collected and conducted to the absorption column described above.

By providing the above-mentioned treated waste water suitable for cleaning barns and pens, the present invention also provides a method for improving the hygiene of stall and barns by cleaning the barns and barns with the recovered spent water. Cleaning includes cleaning and rinsing of stables, floors, roofs, manure drains, ceilings, ventilation ducts, purifying air, and reducing areas that may emit odors, ammonia, and dust into a premeditated area.

In one embodiment of the process of the invention, the cleaning of the stables is carried out with waste water obtained after rotation of the energy boxes or after digestion to separate the solid and liquid materials with biogas production or as a result of subsequent processes in the system.

The methods of the invention make it possible to raise the standard of living of the animals in the barn by using straw in the barn, since the straw serves both as a cage material, a bed material and a structural feed. It is advisable to transfer the organic material straw from the barn to the high pressure lime machine and hydrolyze the organic material there before further processing. Improving the quality of life of the animals housed in the barn is also achieved by allowing the animals to be sprayed in order to reduce the amount of microbes and dust on the hair of the animals while also reducing the body temperature of the animals.

The present invention also provides a process for integrating anaerobic digestion of organic fertilizers, energy crops and other organic matter, and refining the nutrients stored in the digested biomass into commercial grade fertilizers, and producing pure wastewater.

.ϊ », '

87 The aforementioned Integrated Process requires the development of a multi-component system comprising

1) a first device, preferably a barn or shed for keeping and / or rearing animals, jhMMeat pigs, cattle, lees, goats, sheep, poultry, and / or ii) a second device, preferably at least one pre-treatment unit for organic material. a plant containing organic matter preferably containing grain manure and / or animal slurry and / or plant parts, the plant parts containing straw, plants, crop residues, silage or energy plants, and the organic matter being carcasses or parts thereof, slaughterhouse waste, and contains stumps, blood plasma or any other animal product which is BSE prions or other prions. depending on its possible presence, hazardous or non - dangerous substances, and / or

(Iii) a power plant generating a significant amount of energy from a biomass containing the organic material, the first device comprising:

(a) a system for cleaning floors, roofs, cabins, sewers, sludges or screens, and ventilation ducts for buildings or sheds for animals, which use purification water from a fistula system; and / or

(b) a system for conveying fresh water from the buildings or stables of the animals to the second device in the form of a slurry of organic water and organic matter;

wherein the second device contains

a) a first pretreatment tank, preferably an extraction tank, in which i) nitrogen is removed from the slurry conveyed from the first device to the second device, or 11) nitrogen is removed from the organic material from the auxiliary pre-treatment vessel, Hfetwe ammonia wherein the first pretreatment tank can be used to hydrolyze the organic material and / or

(b) a second high-pressure lime digestion unit containing egv second pretreatment tank, preferably from the first device to the second device, for hydrolysis of the slurry, wherein the hydrolysis is viable microbial organisms and / or pathogenic materials in the slurry. ♦ ♦ χ ♦ * results in quantitative reduction and / or inactivation and / or complete destruction, and / or

(c) at least one container, preferably a silo container, which produces at least one of the following: wheat, maize, energy crops, sugar beet and vegetable residues; and or

d) at least one second container, preferably a pretreatment digestion tank for silage and / or organic material treated with high pressure lime, wherein the digestion can be done by mesophilic digestion and / or natural digestion;

where the third device contains

(a) at least one biogas producing digestion tank into which the slurry and / or organic material can be introduced from the second device and which digest the organic material by mesophilic digestion and / or natural digestion which results in the production of biogas containing mainly methane; and or

(b) at least one biogas storage tank, which is connected to a biogas outlet or connected to a gas engine; and or

c) at least one first separator, preferably a decanter centrifuge, in which the digested material from the at least one biogas producing digestion vessel is separated into a substantially liquid fraction and a substantially solid fraction formed from residual water comprising a solid fraction of organic and inorganic solid phosphorus materials. available; and or

d) at least one second separator, preferably a ceramic microfilter, wherein the residual water from the at least one first separator is further treated, preferably by aeration and filtration, wherein the treatment comprises at least a portion of the odorous components, nitrogen compounds, and luminescent compounds. removes residual water resulting in the separation of residual water, which contains a reduced amount of odorous compounds, nitrogen compounds, and rumaceous compounds compared to prior separation,

Preferably, the system of the present invention includes pipelines that form a closed system that prevents dust, a | organisms, ammonia, air, liquids, or any other component of the system, resulting in reduced release into the environment of juveniles.

X * «φ V« «* A · ί '

The liquid fractions or waste water from one or more of the at least one skid, the at least one pretreatment rotary tank, the at least one biogas generating digester, the at least one first separator and the at least one second separator are preferably reused for cleaning sheds or barns.

The slurry separation and biogas production system is preferably reusable from one or more of the at least one silo, the at least one pretreatment digestion tank, the at least one biogas producing digestion tank, the at least one first separator and the at least one second separator. any step of maintaining the organic material in a suitable liquid state.

The system makes it possible for you to whitewash ^! : add calcium oxide and / or calcium hydroxide to the organic matter before introducing the organic material into a nitrogen (2W) ammonia extraction tank by adding sufficient lime to the organic material to provide a pH of about 10 k

Change to 12. This step is combined with heating and slurry containing organic matter

Is the grain preferably 5-10 days, 'Pete'? days in the system recovery tank. The temperature inside the stripper tank is preferably between 68 ^o C and 8CPC. To the organic material in the extraction vessel, 30-80 g Ca (H) per kg of dry matter in the organic material is added before the organic material is introduced into the extraction vessel.

The system makes it possible to collect the extracted nitrogen, ammonia ammonia, and to transfer the extracted nitrogen to a column in which the nitrogen, HfÉve bb ammonia, is absorbed in water or in an acidic solution, preferably containing sulfuric acid and then, if necessary, an absorbed ammonia. store in a container. Nitrogen is preferably absorbed in water or in an acidic solution

The high pressure lime cooker forming part of the system is a device which is initially suitable for slicing the grain material and then for transferring the sliced organic material to a chamber where the chopped organic material is heated and treated at high temperature and high pressure. To the organic material to be treated in the high-pressure lime stove, a predetermined amount of lime, live calcium oxide and / or calcium hydroxide is added before or after it is introduced into the high-pressure lime machine.

♦ *

The high pressure lime boiler is preferably introduced at a volume of 5 to 10 g per kg of dry matter in the organic system, operating at a temperature between KMFC and 220 ° C, at a temperature of about 200 ° C to about 100 ° C. The temperature is adapted to the organic material to be treated and a higher temperature is used when the organic material contains a higher amount of cellulose, bisylcellulose or 11gr, even if there is a risk of infecting microbial organisms or pathogens such as BSE in the organic material. there are pdonos.

The pressure is 2x10 ⁵ Pa and preferably ^1,8χ10 δ between Pa, Pa ö 4-16x1, my example 8-16x10 Pa ^s,

5-18 x 10 ^s Pa, The system operates at elevated temperature for about 5-18 minutes, but also for prolonged treatment

The nitrogen extracted in the high-pressure lime machine is preferably collected and discharged to a column where it is absorbed as described above.

One embodiment of the system of the present invention allows for the removal of silage, such as maize, energy crops, sugar beet and / or crop residues, into a mesophilic or naturally rotting container before transferring the material to the extraction tank. The system of the present invention also allows the organic material treated in the high-pressure lime machine to be fed to a field or their product in a digestion tank before being fed to the extraction tank.

The system of the present invention also helps optimize organic matter digestion and biogas production by providing a pretreatment system in which nitrogen is eliminated and / or alkaline hydrolysis can be performed at predetermined parameters such as pH value, temperature, aeration, duration:, antifoam and fluffiness of suspended materials.

Another embodiment of the system of the present invention provides optimal conditions for microbial organisms in biogas-producing digesters. This is achieved by, for example, removing the disinfected or purified slurry from the extraction tank to the at least one first biogas producing digestion vessel which does not inhibit or damage the activity of the biogas producing microorganisms. In particular, the organic matter from which nitrogen, except ammonia has been extracted, may be removed as biogas; * * X * ♦ * ♦ * $ *. * * * *. ».» »« * - «· * * * ♦ ♦ * · ~ 71 production reactors in which digestion conditions are advantageous for mesoilic digestion. After mesophilic rotation of the organic material, the organic material is preferably discharged to another biogas-producing reactor in the system where digestion conditions are suitable for its production! roíhasziásra.

Yours! reaction conditions include: -fume temperature 45-75 * 0, exemplified by a temperature of 55-550 ° C. The mesophilic reaction conditions include the following: ^e rtrerötbetöf 2 O 45 C temperature, e.g. Aörutfc ^ five-30SS temperature.

The system makes it possible for all the fruits! the reaction and the mesolyl reaction were either delayed for at least 5 to 15 days, or for at least 7 to 10 days, preferably at least 7 days.

The system of the present invention also includes devices to prevent foam formation which are suitable, for example, for the addition of polymers and / or vegetable oils, including rapeseed oil and / or salts containing calcium hydroxide and calcium hydroxide.

The system of the invention allows the digested organic material generated in the biogas-producing reactors to be reused at least in part in the same reactor where the digested organic material serves as an inoculum for the Organic Muscle of the -T-T ridge.

One embodiment of the system of the present invention allows the slurry containing the liquid containing the solids to be fed to a first separator which separates solids containing a fraction of the liquid from the bulk of the liquid fraction. The mainly solid fraction contains organic and inorganic materials such as phosphorus and mixtures thereof. The mainly dry fraction can be further dried and used as fertilizer. Preferably, the first separator of the system is a decanter centrifuge.

The system of the present invention further allows the residual water from the first separator to be treated in a second separator, wherein the second separator comprises ceramic microfilters that allow the wastewater from the first separator to be further treated by aeration and filtration, filling as necessary to remove residual odors. , by removing residual nitrogen compounds and / or residual potassium-containing materials, which results in substantially pure wastewater which is substantially free of any residual material.

♦ ♦

The system of the present invention allows waste water from the fermophilic biogas reactor or the first and / or second separator to be discharged to arable land, including the wastewater or wastewater treatment plant or, if necessary, to a biological treatment plant for further purification. .

The system of the invention. The sHefve procedure can be used for the following purposes:

- dust, microorganisms, ammonia, contaminated air, liquid or

Arc · any other component of the system, in particular the reduction or elimination of emissions of materials from the petrol station;

- improving the use of energy in biomass containing organic material;

- enhancing the production of biogas containing methane gas and methane carrier gas. The gas in question may be stored in a tank on site and / or discharged through a gas pipeline network;

- nitrogen, phosphorus, optionally potassium, separated from the organic material. These fractions are well marketed and can be used as fertilizers for fertilizing agricultural and horticultural crops;

- improving the hygiene of the stables and the quality of life of the animals, in line with the output from the stables. Such an output material pethane is the organic slurry as well as the trimmings you have to cut. Keeping animals clean can reduce the risk of contamination of the meat if the animals are slaughtered;

- the conversion of animal carcasses or parts of animal bodies, meat and bone meal and other products of animal origin into refined fertilizers for application to agricultural land and thus the use of micro and macro nutrients in animal products for the production of agricultural and horticultural crops.

Claims (4)

1 :. Method for reducing the number of viable microbial organisms and / or prions in organic material I) collecting organic material containing solid and / or liquid parts; ii) performing the following steps on the organic material; (a) controlling the organic material by high pressure lime treatment at a temperature between 10 ° C and 220 ° C, where the lime is calcium hydroxide and / or calcium oxide; b) extracting the ammonia from the organic material treated with high pressure lime brine; wherein the lime added to recover the ammonia and disinfect the organic matter precipitates with dissolved orthophosphates; (Iii) preparing processed organic material containing reduced amounts of viable microorganism and / or prion; and * X '* iv) feeding the processed organic material into a biogas producing digestion tank (13, 14, 15, 106, 206) in which the processed organic material is digested to produce biogas, 2, The process of claim 1 wherein the processed organic material (sfk ' ₅ I4 ₍ phobic <<- WoTu.vene, M 5 VΛ '··' · '«' V 3. The process of claim 1, wherein the residual material resulting from digestion of the processed organic material is disposed of in an agricultural area. 4. The method of claim 1, wherein the r re, / oranisms are pseudoranges 5. The method of claim 1, wherein the microbial organisms are infectious microbial organisms, parasitic pathogenic microbial organisms. »♦» -748. The process according to claim 1, wherein the organic material comprising the solid and / or liquid moieties is selected from the group consisting of organic fertilizers or their sludges, vegetable residues, carcasses or parts of animals, slaughterhouse waste, meat and bone meal, and any combination thereof. Process according to claim 1, characterized in that during the biogas production, the organic material is treated in a high pressure lime digestion unit (9) before the ammonia is extracted therefrom in an extraction tank (12,102,202,302,402). 8. The process of claim 7, wherein the organic material treated with high pressure lime pellets is decanted prior to the removal of ammonia. 9. A process according to claim 1, wherein the organic material of plant origin is subjected to silage treatment before the removal of ammonia. 10. A process according to claim 9, wherein the plant-derived saline organic material is eluted before the ammonia is extracted. 11. A method according to Claim 7, characterized in that the extraction of ammonia is carried out by first treating 4 O ^ö predetermined quantity of lime is added at a temperature above the C to achieve the organic material more than 9 pH value. The process according to claim 11, wherein the pH is raised above 10. 13. The process of claim 11, wherein the pH is raised above 11. 14. The process of claim 11, wherein the temperature is above 50 ° C. xx Φ Φ ¹ <· '♦ ® Φ »« * Φ * X χ χ · χ ♦ * «* φ φ» ^χ »» * Φ κ> φ »*« The process according to claims 15 to 11, wherein the temperature is above 60 ° C. The process according to claim 11, wherein the ammonia is extracted within 2 to 15 days. 17. The process of claim 11, wherein the ammonia is extracted within 4-10 days. 18. The process of claim 11, wherein the ammonia is extracted within 6-8 days. The process according to claim 7, wherein the pH is 8-12, the temperature is 70-850 ° C, the liquid-gas ratio is less than 1: 400, and the ammonia extraction time is 7 days. 20. The process of claim 11, wherein the organic material is up to 50% w / v solids. 21. The process of claim 11, wherein the organic material is up to 30% w / v solids. 22. The process of claim 11, wherein the organic material is up to 10% w / v solids. A process according to claim 11, characterized in that, before storing the recovered ammonia in a container (23), an ammonia is absorbed The process of claim 23, wherein the ammonia absorption unit (21) comprises water or an acidic solution. 25. A process according to claim 24 wherein the acidic solution is sulfuric acid. ..- « X * Process according to claim 23, characterized in that the ammonia recovered from the high pressure lime cooking is also absorbed in an ammonia absorption unit (21). before being stored in a container (23). 27. Process according to any one of claims 1 to 3, characterized in that the treatment of the organic material in a high pressure lime pot (9) is carried out at a temperature of 12 to 220 ° C and a pressure of 2 to 20 x 10 0 Pa and adding lime to the organic material. and high pressure lime for at least 1 minute and up to 60 minutes. A process according to claim 27, wherein the treatment is carried out at 180200 ° C, a pressure of 1-1.6 x 10 3 Pa and a pH of 10-12, and the treatment is carried out for 5-10 minutes in a high pressure lime deposit (9). . 29. The method of claim 27 wherein the organic material is deep litter, cattle manure, pig manure or poultry manure. 30. The method of claim 27, wherein the organic matter contains BSE prions or other prior proteins, the BSE prions or other priorities being completely destroyed during high pressure lime cooking. 31. The method of claim 27, wherein the organic material also comprises straw, fibers or particulate matter. 32. The method of claim 27, wherein the organic material comprises more than 10% w / w of fiber. 33. The method of claim 27, wherein the organic material comprises more than 10% w / w of complex carbohydrates, including cellulose and / or hemicellulose and / or lignin. · - ♦♦ * V φ> 's ν> · Χ 34. The method of claim 27, wherein 2-80 g of calcium oxide are added to the organic material per kg of dry matter. 35. The method of claim 27, wherein 5-50 g of calcium oxide per kg of dry matter are added to the organic material. 36. The process of claim 27, wherein the organic material is loosened prior to treatment in the high pressure lime digester (9). 37. The method of claim 36, wherein the organic material is loosened by a conveyor auger with which the organic material is conveyed to the high-pressure lime brewing unit <9, 103, 203, 303, 403}, wherein the organic material is steam injection, or by steam or a combination of the two in a jacket located on a stone of high pressure lime cooking unit (9, .103.203, 303,403). A process according to claim 27, wherein the organic material treated in the high pressure lime digestion unit (9) is fed to an digestion vessel (13, 14, 15, 186, 206), wherein the organic material is mesophilic and / or we are actually rotting. 39. The method of claim 38, wherein said rotting bacteria is present. 40. The method of claim 38, wherein the digestion is performed anaerobically. 41. The method of claim 38, wherein the organic material of animal origin contains more than 10% w / v nitrogen. 42. The method of claim 38, wherein the digestion step is higher than ~ 15 ^° C, but carried out at 65 ~ ^c C lower than temperature. 7843rd method according to claim 38, characterized in that the digestion step above 25 ° C, preferably less than 55 at a temperature of ^c. 44. The process according to claim 38, wherein the digestion is carried out at a temperature higher than 3S'-C but lower than 45 ° '. 45. The method of claim 38, wherein the organic material is digested for 5 to 15 days. 46. The method of claim 38, wherein the organic material is digested for 7 to 10 days. 47. The method of claim 9, wherein the organic material to be skied comprises annual sugar crops, especially sugar beet, corn and alfalfa, and optionally green vegetables of said plants. A process according to any one of claims 1 to 11, wherein the biogas production is carried out in one or more rotary tanks (13,14, 15, 1.06, 206) with microbial organisms and the organic material is digested anaerobically. 49. The process of claim 48, wherein the microorganisms used to digest the organic matter are bacteria that are predominantly methane and have a lower carbon dioxide content than methane. The process of claim 48, wherein the biogas production is carried out by digestion of the organic matter with anaerobic bacteria (13, 14, 15, 108, 208), wherein the organic material is in the first rotaphase container (13, 14, 15). , 108, 2Q8) is first digested with thermo bacteria and then the organic material digested with thermo bacteria is transferred to a second digestion tank (13, 14, 15, 108, 208) where it is digested with mesophyll bacteria. 51. The process of claim 50, wherein the thermo reaction is carried out at a reaction temperature of 45-75 ° C. * χ · «* »X * ♦ * -79- ♦ * «* X y «· ♦ ♦ * * ♦ ♦ * * ♦ 52. e A process characterized in that a thermophilic The reaction is carried out at a reaction temperature of 55-60 * 0. 53. The method of claim 50, e archery, characterized in that a field reaction at a reaction temperature of 2 ° to 45 ° C carried out. 54. The method of claim 50, wherein the meson! The reaction is carried out at a reaction temperature of 30-35 * 0. 55. The method of claim 50, wherein the crop is rotting for 5 to 15 days. 56. The method of claim 50, wherein the crop edging is performed for 7 to 10 days. 57. The method of claim 50, wherein the field edge is rotated for 5 to 15 days. 58. The process of claim 50, wherein the field edge is applied for 7 to 10 days. 59. The process according to claim 56, wherein any foam formation is reduced and / or completely eliminated by the addition of polymers and / or vegetable oils and / or one or more salts. 60. The method of claim 59, wherein the vegetable oil is rapeseed oil. 61. The process of claim 48, wherein the desired flocculation of the materials and particles during biogas production is achieved by adding calcium ions, which form calcium bridges between the organic and inorganic materials in solution or suspension, hldak cause the particles to flake. tr 82. The method of claim 81, wherein the addition of calcium ions results in the precipitation of ortho-phosphates, including dissolved POZ ions, wherein the PyZ ions are precipitated in the form of calcium phosphate (Ca _g (PO ₄ ) ₂ ), wherein the precipitated calcium phosphate floats in the sludge. 83. The method of claim 81, wherein the biogas is produced in a gas engine (28) capable of generating heat and / or electric current. 84. The process according to claim 83, wherein the heat generated is provided by a high pressure lime brewing unit (9,103,203,303,403) and / or a roleplasting ridge (115,213) and / or an extraction tank (12,102,202). 302,402) and / or for heating one or more biogas producing digestion tanks (13,14,15,106,206) and / or one or more housing or stables for keeping animals (1,101, 201,301,401). 85. The method of claim 83, wherein the electric current is conducted and sold to an electric distribution network. 88. The method of any one of claims 1-11, wherein the microorganism is Campylobacter, Salmonella, Versinia, Ascaris, viruses or viroids. 87. A1-11. A process according to any one of the claims, wherein the organic material is a nitrogenous fertilizer by: i) collecting the ammonia recovered from the organic material in an ammonia extraction step, iii) absorbing the ammonia in water or an acidic solution, preferably sulfuric acid, and finally III) A nitrogenous fertilizer is produced. 83. A 1-11. A process according to any one of claims 1 to 5, characterized in that the organic material is made from bulk organic fertilizers by: -81 Ο from the biogas-producing digester (13, 14, 15, 106, 206) to the first sludge, (a) separating the decomposed organic and inorganic materials into a solid fraction and a liquid fraction containing wastewater, III) Calcium phosphate of the formula GaaCPCMa. and preparing a solid fraction partially containing phosphorus in the form of organic phosphates, wherein the solid fraction is a solid; fraction can be used as fertilizer for phosphorus content. 60. The process of claim 68, wherein the separator is a decanter centrifuge (18, 107, 207, 304.404), 78. The method of claim 68, wherein the solid phosphorus-containing fraction is dried and granulated with phosphorus-containing fertilizer. 71. The method of claim 68; A process comprising separating waste water containing less than 0.5% rWV of nitrogen and phosphorus. 72. The method of claim 71, wherein the waste water is discharged to the extraction tank (12, 102, 202, 302) and reused to remove ammonia from the organic material in the extraction tank (12, 102, 202, 302). . 73. The process of claim 71, wherein the waste water is reused for cleaning pens or stables (101, 201, 301, 401). 74, The method of claim 71 szerínfí, azzal.jellemezve to the reject water contains no sources ameiyélb (álkalmasak.zaa® ^s ^ e ^ e ^ e "A" e ^ infectious bacteria, parasites, BSE and other pnönok 75. The method of claim 68, wherein ammonia is removed from the waste water by a steam extraction device (20). ? 76. The method of claim 75, wherein the extracted ammonia is precipitated in a two-stage ammonia absorption unit (21). 77. The method of claim 78, wherein the ammonia is first condensed in a countercurrently cooled ammonia condensate. 78. The method of claim 77, wherein the non-condensing ammonia in the first step is condensed in the reverse stream of a permeate formed during a reverse osmosis filtration step during potassium extraction. 79. The method of claim 75, wherein the extracted ammonia is introduced into an ammonia absorption unit (21) in which ammonia from the extraction tank (12,102,202,302,402) is absorbed. 80. The method of claim 69, further comprising the step of preparing the potassium-containing fertilizer from the organic material by: I) transferring the potassium-containing liquid fraction of the effluent from the kig &gt; clone (29) to a second separation which is carried out in a reverse osmosis filter unit (29), ii) separating the remaining organic and inorganic materials from the liquid fraction. then isi) preparing a potassium-containing liquid concentrate which can be used as a potassium-containing muirua 81. The method of claim 88, wherein in the second separation step, the potassium-containing liquid fraction is passed through an intermittently ventilated ml filter which removes the remaining organic matter by venting to form inorganic flakes. 82, A biogas plant containing solid and liquid parts of biogas. produced by anaerobic digestion of processed organic matter, plant contains i) an extraction vessel (12,102, 202,302,402) for removing ammonia from the organic material treated in the high-pressure lime digester unit, wherein the extraction vessel (12,102, 202,302,402) for absorbing and condensing the recovered ammonia 21 connected, li) a digestion tank (13,14,15,106,206) for anaerobic digestion of organic material treated and pressurized in the high-pressure lime digestion unit, which digestion results in biogas production, characterized in that the plant further comprises a high-pressure lime digestion unit (9); 103, 203, 303, 403) for bridging organic matter, wherein the high pressure lime cooking unit (9,103,203,303,403) and the extraction tank (12,102,202,302,402) are connected by treating the high pressure lime cooking unit organic material can be discharged from the high pressure lime cooking unit (9, 103, 203, 303, 403) to the extraction tank (12,102,202, 302,402), wherein the extraction tank (12,102,202,302,402) and the biogas digestion tank (13,14,15,106,105,205) are interconnected such that the high pressure lime-treated and ammonium amine organic material from the extraction tank (12,102,202,302) 402) a biogas head drainage digester tank (13,14,15,108,200) is provided, and wherein the high pressure lime digester unit (9,103,203,303,403) and the extraction tank (12,102,202,302,402) are further provided. interconnected such that the recovered ammonia from the high-pressure lime digestion unit (0, 103, 203, 303.403) to the extraction tank (12, 102, 202, 302,402) can be transmitted and absorbed in an ammonia absorption unit (21), The widow according to claim 82, further comprising a main receiving vessel (3) for receiving the organic slurry, wherein the main receiving vessel (3) for the high pressure lime brewing unit (9, 103, 203, 303, 403) and connected to an extraction vessel (12, 102, 202, 302, 402) such that the organic slurry from the main receiving vessel (3) to the high-pressure lime brewing unit (9,103,203,303,403) and the extraction vessel (12,102,202) , 302, 402). 84. The widow of claim 83, further comprising a silo tank (7, 104, 204) for storing energy crops. 85. The plant according to claim 83, further comprising a collecting tank (2) for collecting organic material, the collecting tank (2) being connected to the main receiving tank (3) and the collecting tank (2) comprising a pump, pumping the organic slurry from the hopper tank (2) to the main receiving tank (3) for receiving the organic slurry. 88. A widow according to claim 85, characterized in that it comprises a lead or barn (1, 101, 201, 301, 401) for rearing pets, wherein the collecting container (2) is a lead or barn (1, 101, 201, 301). , 401) is placed underneath the floor and is connected to the shed or barn (1, 101, 201, 301, 401) so that the slurry can be removed from the shed or barn (1, 101, 201, 301, 401) by gravity to the slurry collecting container (2). 87. The plant of claim 82 further comprising a mixing vessel (10) for mixing organic material treated with the high pressure lime brewing unit (9, 103, 203, 303, 403) and organic slurry from the main holding vessel (3). ), which mixing vessel (1-0) is connected to the high pressure lime cooking unit (9, 103, 203, 303, 403) and the organic material treated with high pressure lime cooking and the organic slurry from the high pressure lime cooking unit (9, 103, 203, 303) 403) can be introduced into the mixing tank (10), wherein the mixing tank (10) is also connected to the extraction tank (12,102, 202, 302,402). 88. The plant of claim 87, further comprising a lime feed tank (4) which is a sliding tank (4) on a manifold to a high pressure lime cooking unit (0, 103, 203, 303, 403). and the mixing tank. (10) is connected in such a way that the lime is fed from the high pressure lime cooking unit (9, 103, 203, 303, 403) to the mixing tank (10). ♦ «» * X X * ♦ * * * »*« * «* χ. «« < ~ branch .... The plant of claim 88, further comprising a macerator (30) for maceration of the organic material, said macerator (30) for said mixing vessel (10) and said extraction vessel (12, 102, 202). 302, 402) is coupled such that a mixture of organic material treated with high-pressure lime and organic slurry is introduced from the mixing vessel (10) into the extraction vessel (12, 102, 2G2, 302, 402). 90. The plant of claim 89, further comprising a main receiving vessel (3) for receiving the organic slurry, the main receiving vessel (3) for the high pressure lime brewing unit (9, 103, 203, 303, 403), is connected to the tank (12, 102, 202, 302, 402) and the mixing tank (10) such that the organic slurry from the main receiving tank (3) into the high pressure lime brewing unit (9, 103, 203, 303, 403), can be conveyed to a container (12, 102, 202, 302, 402) and to a mixing container (10). 91. The plant according to claim 90, further comprising a collection tank (2) for collecting the organic slurry, the collecting tank (2) being connected to the main receiving tank (3), and wherein the collecting tank (2) comprises a a pump for pumping organic slurry from the collection tank (2) to the main receiving tank (3) for receiving organic slurry. 92. The widow according to claim 92, further comprising a lead or barn (1, 101, 201, 301, 401) for keeping pets, wherein the collecting container (2) is a lead or barn (1, 101, 201, 301, 401) and is connected to the barn or barn (1, 101, 201, 301, 401) so that the slurry from the barn or barn (1, 5, 201, 301, 401) is gravitated can be led to the collection tank (2). 93. The plant according to claim 82, further comprising a lime storage silo tank (4) which is connected to the high pressure lime brewing unit (9, 103, 203, 303, 403) so that the lime is can be conveyed to a high pressure lime cooking unit (9,103, 203,303,403). * ♦ «♦ · * * 94. The plant of claim 82, further comprising a conveying and homogenizing system (8) for conveying and homogenizing the solid organic material, the conveying and homogenizing system (8) comprising conveyor screws and an integrated macerator (30), wherein: The conveying and homogenizing system (8) is connected to the high-pressure lime digestion unit (9, 103, 203, 393, 403) so that the homogenized solid organic matter can be conveyed to the high-pressure lime digestion unit (9, 103, 203, 303, 403). 9S. The plant according to claim 94, further comprising a receiving station (8) for receiving the solid organic material, the receiving station (8) being connected to the floor by conveyor screws and the receiving station (8) being a conveying and homogenizing system (8). is connected to the high pressure lime digestion unit (9, 103, 203, 303, 403) such that the homogenized solid organic material from the receiving station (6) through the conveying and homogenizing system (8) to the high pressure lime digestion unit (9, 103, 203). , 303, 403). 98. The plant of claim 95, further comprising a balance (5) for measuring the mass of the solid organic material. 97. A. The plant of claim 82, further comprising an acid storage tank (22) for storing sulfuric acid, the acid storage tank (22) being attached to the ammonia absorption unit (21) such that the sulfuric acid is can be led to an absorption unit (21). 98, The plant of claim 82, further comprising a tank (23, 210) for removing ammonia extracted from the extraction tank (12, 102, 202, 302, 402) and condensed in the ammonia absorption unit (21). , 303, 408), which container (23, 210, 308, 408) is connected to the ammonia absorption unit (21) such that the condensed ammonia from the ammonia absorption unit (21) is stored in a container (23) for extracting ammonia. 210, 308, 498). * .. .... 8? 99. The plant according to claim 82, further comprising an air primer unit (31) for filtering air from the ammonia absorption unit (21), the air filter unit (31) being connected to the ammonia absorption unit (21). such that air from the ammonia absorption unit (21) can be conveyed to the air freshener unit (31). 100. The plant according to claim 82, further comprising a liquid biomass storage tank (11) for a biogas generating digestion tank (13, 14, 15, 106, 206) and an extractor. is connected to a container (12, 102, 202, 302, 402) such that the liquid biomass from the storage container (11) to the blogging digestion container (13, 14, 15, 188, 208) and the extraction container (12, 102, 202,302,402). 101. The plant of claim 82, further comprising an organic acid reservoir (18) containing an organic acid for adjusting the pH of the organic material stored in the biogas generating digester (13, 14, 15, 106, 208), the acid reservoir (18). 18) is connected to the biogas generating digestion tank (13, 14, T5, 108, 208) so that organic acid can be transferred from the acid storage reservoir (16) to the blog digest digestion tank (13, 14, 18, 108,206). 102. The widow according to claim 82, characterized in that the PAx / hnyyáAítewwwte »*«: 7ηί «& nssffertarfáM n'71» m «h / ni further contains a PAXf plus ⁵ asaph ^? a scavenging buffer vessel (17), which buffer vessel (17) is connected to the blogging digestion tank (13,14,15,108, 206) such that the decomposed and degassed organic material can be conducted from the biogas digesting tank (13,14,15,108). 103. The plant of claim 102, further comprising a decanter centrifuge (18, 107, 207, 304, 404) which separates the decomposed and degassed organic material into a phosphorous semi-solid fraction and an aqueous phase, which is a decanter centrifuge (18, 107, 207, 304, 404) is connected to the buffer tank (17) so that the degassed and degassed and then buffered organic material is transferred from the buffer tank (17) to a decanter centrifuge (18, 107, 207, 304, 404). . · * - * · «·« '♦ 104. The plant of claim 103, further comprising a container (19, 112, 211, 309, 409) for collecting a phosphorus-containing semi-solid fraction from the decanting centrifuge (18, 107, 207, 304, 404). ), wherein the phosphorus-containing semi-solid fraction collection vessel (19, 112, 211, 309, 409) is connected to the decanting centrifuge (18, 107, 207, 304, 404) such that the phosphorus-containing, semi-solid fraction is decanted. from a centrifuge (18, 107, 207, 304, 404) to a container (19, 112, 211, 300, 409) for collecting the phosphorous-containing semi-solid fraction. 105. The plant of claim 103, further comprising a second buffer vessel (32) for buffering the aqueous phase from the decanting centrifuge (18. 107, 207, 304, 404), wherein the second buffer vessel (32) for the decanting centrifuge. (18, 107, 207, 304, 404) is connected such that the aqueous phase is introduced from the decanting centrifuge (18, 107, 207, 304, 404) into a second buffer tank (32), 103. The plant according to claim 105, further comprising a lead or barn (t, 101, 201, 301, 401) for keeping pets, wherein the second buffer container (32) for the lamb or barn (1, 101, 201, 301) , 401) is connected in such a way that the buffered water phase can be introduced from the second buffer tank (32) into the shed or barn (1, 101, 201, 301, 401). 107. The plant of claim 105, wherein the second buffer tank (32) is connected to the extraction tank (12, 102, 202, 302, 402) such that the buffered water phase from the second buffer (32) is into the extraction tank. (12, 102, 202, 302, 402). 108. The plant according to claim 105, further comprising a steam stripping column (20) for removing residual ammonia from the aqueous phase from the decanting centrifuge (18, 107, 207, 304, 404), which is a steam stripping column (20). connected to a second buffer vessel (32) such that the buffered water can be conveyed from the second buffer vessel (32) to the steam evaporation column (20). 89109. The carbonaceous carbon of claim 105, wherein the dilution column (20) is connected to the ammonia absorption unit (21) such that the ammonia extracted from the extraction column (29) is incorporated into said ammonia absorption unit (21). traced. 170. The plant according to claim 105, further comprising a waste water tank (25, 214, 371, 407) for collecting ammonia water in the tanks (20) and collecting the buffered water in the second buffer vessel (32). comprising a sludge reservoir (25, 214, 311, 407) connected to the dilution column (20) and the second buffer tank (32) such that water from the stripping column (20) and buffered water from the second buffer reservoir (32) are wastewater. container (25, 214, 311, 407). 117, The widow of claim 110, further comprising a lead or barn (1, 701, 201, 301, 401) for keeping pets, wherein the waste water reservoir (25, 214, 311, 407) connected to the barn (1, 101, 201, 307, 401) such that the waste water can be led to the barn or barn (1, 101, 201, 301, 401). 772. A widow according to claim 710, characterized in that said waste water tank (25, 214, 311, 407) is connected to the extraction tank (12, 102, 202, 302, 402) such that the waste water is the extractor. can be introduced into a container (12, 102, 202, 302, 402). 713. The furnace of claim 110, further comprising a reverse osmosis filtration unit (29) for separating potassium from the effluent reservoir (25, 214, 311, 407), which is a reverse osmosis filtration unit (29). 29) is connected to the waste water tank (25, 214, 311, 407) such that the waste water from the waste water tank (25, 214, 317, 407) can be conveyed to the reverse osmosis filter unit (29). 114. The plant of claim 173, further comprising a potassium solution collecting vessel (26, 173, 370), wherein the potassium solution collecting vessel (26, 113, 310) is provided for the reverse osmosis filter unit. (29) ♦ * ♦ ♦ «*« φ φ ♦ * * ♦ * φ χ *** <* ♦> X χ _χ A ν * -90 contacting means such that the pulp concentrate from the reverse osmosis filter unit (29) can be introduced into a container (26, 113, 310) for collecting the potassium solution. 115. The widow according to claim 82, further comprising a condensate drainage unit (33) in the biogas produced by anaerobic digestion of the organic matter, which is connected to the biogas generating digester (13, 14, 15, 106, 106). wherein the biogas produced by anaerobic digestion of the digestion tanks (13, 14, 15, 106, 206) is transported from the biogas generating digestion tank (13, 14, 15, 108, 208) to the condensed water storage unit (33). 115. The widow of claim 115 further comprising a gas container (24) for storing biogas produced by anaerobic digestion of the organic material, the gas container (24) being connected to the condensed water storage unit (33) such that the biogas can be transported from the condensed water storage unit (33) to the gas tank (24). 117, The plant of claim 118, further comprising a gas scrubbing unit (27) for purifying the biogas produced therefrom, the gas cleaning unit (27) being connected to the gas tank (24). the biogas may be introduced from the gas reservoir (24) into the gas purification unit (27). 118. The widow of claim 117, further comprising a combined heat and power plant (28) for burning biogas and producing electricity and heat, said combined heat and power plant (28). connected to the gas purification unit (27) so that the purified gas can be conveyed from the gas purification unit (27) to the combined heat and power plant (28). 119. The plant of claim 82, further comprising (iv) a lead or barn (1, 101, 201, 301, 401) for keeping domestic animals, wherein the organic slurry from the edge or barn (1, 101, 201, 301, 401). the high pressure «> It can be conveyed to a lime cooking unit (9, 103, 203, 303, 403) and / or to an extraction tank (12, 102, 202, 302,402); v> a recovery tank (23, 210, 303, 408) previously collected in the extraction tank (12, 102, 292, 302, 402), wherein the ammonia collection tank (23, 210, 308, 408) and the extraction tank (23, 210, 308, 408) 12, 1-02, 202, 302, 402) are coupled to each other in such a way that the recovered ammonia from the extraction tank (12, 102, 202, 302, 402) can be transferred to the aroma collection tank (23, 210, 308, 408); (vi) a silo (7, 104) for storing the rotting organic material in silo; 204); vii) an anaerobic pre-treatment digestion tank (115, 213) for anaerobic digestion of the silo to remove the biogas in the silo, wherein the anaerobic pre-digestion tank (115, 213) for the silo container. (7, 104, 204) is coupled such that the slider is guided from the silo tank (7, 104, 204) to the anaerobic pre-treatment tank (115, 213), and wherein the anaerobic rotator tank (115, 213) to the extraction tank (12, 102, 202, 302, 402) is coupled such that the dewatered silo can be conveyed from the anaerobic pretreatment digester tank (115, 213) to the extraction tank (12, 102, 202, 302, 402); vili) a decanting centrifuge (18, 107, 207, 304, 404) for separating the solid and liquid components, wherein the decanting centrifuge (18, 107, 207, 304, 404) is provided to the biogas head drainage container (13, 14, 15, 105); 206) is coupled to anaerobic digestion of high pressure lime treated and de-ammonia organic matter, such that the previously pressurized lime-de-leached and ammonia-free, then decanted organic material is contained in a biogas generator digester (13, 14, 15, 207, 304, 404); (xx) a solid fraction collection vessel (10, 112, 211, 309, 409) for phosphorus-containing walls produced by decanter centrifugation, wherein the phosphorus-containing semi-solid fraction collection vessel (19, 112, 211, 309, 409). and the decanting centrifuge (18, 107, 207, 304, 404) is coupled to each other such that the phosphorus separated from the decanting centrifuge (18, 107, 207, 304, 404) into a phosphorus-containing semi-solid fraction collection vessel (19, 112, 211). , 309, 409) can be driven; and x) a liquid fraction (25, 214, 311, 407) receiving the liquid fraction in the form of effluent from the centrifuge of the decanter, where the rneddov water tank (25, ♦ X) -92214, 311, 407} and the decanting centrifuge (18, 107, 207, 304, 404) are connected such that the waste water from the decanting centrifuge (18, 107, 207, 304, 404) to the fresh water tank (25). , 214, 311, 407). 120. The plant of claim 119, further comprising a gas engine (28), wherein the gas engine (28) and the biogas generating digester (13, 14, 15, 108, 206) are coupled such that the biogas from the digestion tank (13,14,15,106,206,208) of the biogas generator can be fed to the gas engine (28). 121. The plant of claim 82, further comprising (iv) a house or barn (1,101, 201, 301, 401) for keeping pets, wherein the house or barn (1, 101, 201, 301, 401) comprises (a) a clean water purifier system for cleaning the sewers of the shed or barn (1, 101, 201, 301, 401); (b) ventilation ducts; and c) slurry of organic matter from the lead or barn (1, 101, 201, 301, 401) to the high pressure lime digestion unit (9, 103, 203, 303, 403) and / or to the extraction tank (12, 102, 202, 302, 402); which are arranged such that the organic slurry from the barn or barn (1, 101, 201, 301, 401) to the high pressure lime digester (9, 103, 203, 303, 403) and / or to the extraction tank (12, 102) , 202, 302, 402) may be transmitted; (v) a silage reservoir of slated material produced from energy crops (7, 104, 204); (vi) the silage and / or organic material treated with high pressure lime is mesophilic or produced! a digestion pre-treatment digestion tank (115, 213), wherein the pretreatment digestion tank (115, 213) is connected to the silo tank (7, 104, 204) and the high pressure lime digester (9, 103, 203, 303, 403) so that the silo or high pressure lime cooked material can be transferred from the silo tank (7, 104, 204) or the high pressure lime digester unit (9, 103, 203, 303, 403) to the anaerobic pretreatment digester (115, 213), and wherein the anaerobic pretreatment digester (115, 213) is also connected to the extraction tank (12, 102, 202, 302, 402) so that it can be digested in silage or high pressure lime ♦ φ .... Q3 treated organic material may be introduced from the anaerobic pretreatment digestion tank (13, 14, 15, 106, 206) to the extraction tank (12,102,202,302,402); vil) a decanting centrifuge (18, W7, 207, 304, 404) in which the organic matter produced by the digestion of biogas is decomposed into waste water and a solid fraction containing phosphorus-containing organic and inorganic material, wherein the decanting centrifuge (13, 107, 207). 304, 404) is connected to a biogas digestion tank (13, 14, 15, 106, 206) for the anaerobic digestion of organic matter treated with high-pressure lime and ammonia-demineralized and pre-digested biogas 13, 14, 15, 106, 206} to the decanting centrifuge (18, 107, 207, 304, 404); vili) a filter unit (20) comprising a ceramic microfilter for separating residual solids from the effluent during decanting centrifugation, wherein the ceramic microfiltration filter unit (29) is connected to the decanting centrifuge (18, 107, 207, 304, 404) by and (ix) a blogase collecting gas vessel (24), wherein the gas vessel (24) is connected to the biogas digestion vessel (13, 14, 15, 106, 208) in such a manner that the biogas formed by the digestion of the lime-treated and ammonia-free organic matter from the digestion tank <13, 14, 15, 106, 208) to the gas tank (24); 28) Connected. 122, A fluid according to claim 82, wherein the ammonia absorption unit (21) is connected to an acid storage vessel (22) from which sulfuric acid can be introduced into the ammonia absorption unit (21), wherein the ammonia absorption unit (21) connected to a depleted ammonia storage tank (23, 210, 308, 408) such that condensed ammonia can be introduced into and stored in the depleted ammonia storage tank (23, 210, 308, 408) where the condensed ammonia storage tank (23, 210, 308, 408} having a condensed ammonia outlet, and wherein the ammonia absorption unit (21) is connected to said extraction tank (12, 102, 202, 302, 402), and wherein the plant further comprises φ «♦ * ί ♦ - 94 livestock sheds or stalls (1,101, 201, 301, 401>; a collection container (2) for collecting organic slurry from a lead or barn (1, 101, 201, 301, 401); wherein the slurry collection container (2) is located below the floor of the shed or barn (1, 101, 201, 301, 401) and is connected to the shed or shed (1, 101, 201, 301, 401) such that the waste water from the stew or barn (1, 101, 201, 301, 401) by means of gravity to the collecting tank (2), and wherein the slurry collecting tank (2) comprises a pump for connecting the organic slurry from the collecting tank (2) via a connection, for transferring the organic sludge to the main rotating tank (3), and wherein the receiving tank (3) for the high-pressure lime digestion unit (9, 103, 203, 303, 403), the extraction tank (1.2, 102, 202, 302); 402) and is connected to a ski container (7) for storing plant material produced by sliding energy plants; a mixing vessel (10) for mixing the organic material treated with high pressure lime, wherein the mixing vessel (10) is further connected to the high pressure liming unit (9, 103, 203, 303,403), and wherein the organic material and organic slurry treated with high pressure lime from the lime cooking unit (9, 103, 203, 303, 403) and from the main receiving vessel (3) to the mixing vessel (10), whereby the mixing vessel (10) passes through an organic maceration macerator (30) to the extraction vessel (12). , 102, 202, 302, 402) such that the mixture of organic material treated with high pressure lime and organic slurry, after macerating, can be introduced from the mixing vessel (10) into the extraction vessel (12,102,202,302,402), wherein the main receiving vessel (3) a pump for transferring organic slurry from the main receiving tank (3) to the high pressure liming unit (9, 103, 203, 303, 403) and / or pumping it into a drinking tank (12, 102, 202, 302, 402) and / or mixing tank (10); ♦ »χ-95 a slide vessel (4) for distributing crawls to the high pressure lime brewing unit (9, 103, 203, 303, 403) or to the mixing tank (10); a balance (5) for measuring the mass of solid organic matter; a ski storage tank (7, 104, 204) for producing silage plant material using energy plants; a solid organic material receiving station (8), wherein the receiving station (8) is connected to the floor by conveyor screws, and wherein the receiving station (6) is connected to the high pressure lime brewing unit (9, 103 to 203) through a conveying and homogenizing system (3); 303, 403), which homogenizes solid 7 <5 organic material from the receiving station (6), to a -fewfa high-pressure lime digestion unit (9,103, 203, 303, 403), and wherein the conveying and homogenizing system (8) conveyors and an integrated includes a macerator (30) ;: a liquid biomass storage tank (11), wherein the liquid biomass storage tank (11) is connected to the biogas generation digestion tank (13, 14, 15, 106, 206) and the extraction tank (12, 102, 202, 302,402) by: the liquid biomass can be introduced from the liquid biomass storage tank (11) into the biogas generator digestion tank (13, 14, 15, 106, 208) and into the extraction tank (12, 102, 202, 302, 402); an organic acid reservoir for adjusting the pH of the organic material in the biogas generator digester (13, 14, 15, 108, 208). (16) wherein the acid reservoir (18) is connected to the biogas generating digestion tank (13, 14, 15, 108, 205) so that the organic acid can be introduced into the biogas generating digestion tank (13, 14, 15, 108, 208); a decanting centrifuge (18, 107, 207, 304, 404) separating the decomposed and degassed organic material into a phosphorous semi-solid fraction and an aqueous phase, wherein the decanting centrifuge (18, 107, 207, 304, 404) is provided through a buffer container (17). PÁX ♦ is connected to the digestion tank (13, 14, 15, 106, 206) * ♦ 96 / D, so that the degassed and decomposed organic material is introduced from the digestion tank (13, 14, 15, 106, 206) of the biogas generator into the buffer tank (17) and the organic buffer from the buffer tank (17) into the decanting centrifuge (18). 107, 207, 304, 404), wherein the buffer tank (17) comprises a pump for transferring the decomposed and degassed organic material from the buffer storage (17) to the decanting centrifuge (18, 107, 207, 304, 404). and wherein the decanting centrifuge (18, 107, 207, 304, 404) is in a decanting centrifuge (18, 107, 207, 304, 404) for collecting a phosphorus-containing, semi-solid fraction collection vessel (19, 112, 211, 309, 409) is coupled such that the semi-solid fraction is introduced into the phosphorus-containing semi-solid fraction collection vessel (19,112, 211, 309, 409); a gas container (24) for storing biogas produced by anaerobic digestion of organic material, wherein the gas container (24) is connected to said digestion tank (13, 14, 15, 106, 200) such that the digestion container (13, 14, 15, 100) 206) the biogas produced by anaerobic digestion can be introduced into the gas reservoir (24) via a condensate water storage unit (33) in the biogas formed during anaerobic digestion, wherein the condensate water storage unit (33) is provided to the biogas digester digester 15, 206) and is connected to the gas container (24) so that the biogas is fed from the biogas purification digester (13, 14,15, 106, 206) to the condensate storage unit (33) and then to the gas container (24), where 33) an outlet through which condensate from biogas can be removed from the plant; a gas purification unit (27) for purifying the biogas produced from traces of hydrogen sulphide prior to incineration of the biogas, wherein the gas purification unit (27) is connected to the gas reservoir (24) so that the biogas from the gas reservoir (24) ) can be driven; at a combined heat and power plant burning biogas, wherein the combined heat and power plant (i28) is connected to the gas purification unit (1) such that the purified biogas from the gas purification unit (27) can be fed to the combined heat and power plant; , whereby the combined heat and power plant (28) generates electricity by burning the shale gas, which can be fed to a utility electricity distribution network, whereby the biogas combustion also generates heat generated by said combined heat and power. (28) can be used for cooling by means of a circulating system, and wherein the heat absorbed by the circulating system is the high pressure lime brewing unit (9, 103, 203, 303, 403), the extraction tank (12, 102, 202, 302, 402), used for heating the rotating container (13, 14, 15, 108, 206) and / or the shed or barn (1, 101, 201, 301, 401); a stripping column (20) for extracting residual ammonia from the aqueous phase produced in the decanting centrifuge (18, 107, 207, 304, 404), wherein the stripping column (20) comprises one. a steam-water heat exchanger heated to the combined heat and power plant? (28) and wherein the stripping assembly (20) is connected to a decanter centrifuge (18, 107, 207, 304, 404); ), such that the aqueous phase produced in the decanting centrifuge (18, 107, 207, 304, 404) can be introduced into the flushing column (20) and wherein the stripping column (20) is also connected to the ammonia absorption unit (21) the ammonia recovered in the vaporization column (20) can be introduced into the ammonia absorption unit (21) and wherein the decanting centrifuge (18, 107, 207, 304, 404) and the desulphurisation column (20) are connected via a second buffer vessel (32); wherein the second buffer vessel (32) is connected to the decanting centrifuge (18, 107, 207, 304, 404) and to the stripping column (20) such that the aqueous phase produced in the decanting centrifuge (18, 107, 207, 304,404) from the decanting centrifuge (18). 18, 107, 207, 304, 404) can be introduced into the second buffer container (32), and further, the buffered fluid phase is introduced from the second purge container (32) into the dilution column (20), wherein - the second buffer container (32) is also connected to an outlet container (12, 102, 202, 302, 402) and to a shed or barn (1, 101, 201, 301, 401) such that the decanter is centrifuged (18, 107, 207, 3G4, 404). water can be introduced into the extraction tank (12, 102,202, 302, 402) and into the shed or barn (1, 101, 201, 301,401); a waste water tank (25, 214,311,407) for collecting waste water from ammonia and water from a decanter centrifuge (18, 107, 207, 304, 404) in a second concentration tank (32) for collecting water from a scavenger tank (32); , 214, 311, 407) is connected to the purge column (20) such that the water recovered for the ammonia is the heat of the purge column! can be introduced into the waste water tank (25, 214,311,407), and wherein the waste water tank (25, 214, 311, 407) is also connected to the second buffer tank (32) so that the decanting centrifuge (18, 107, 207, 304) 404) can be introduced into said waste water tank (25, 214, 311, 407) through said second buffer tank (32), and wherein the waste water tank (25, 214, 311, 407) is directed to the extraction tank (12, 102, 202). 302, 402) and to the stall or barn (1, 101, 201, 301, 401) such that the waste water from the waste water tank (25, 214, 311, 407) is discharged into the extraction tank (12, 102, 202). , 302, 402) and can be led to a barn or barn (1, 101, 201, 301, 401); a reverse osmosis filtration unit (29) for removing potassium from the effluent reservoir (25, 214, 311, 407), wherein the reverse osmosis filtration unit (29) comprises (a) a ceramic microfibre; and b) an inverse osmosis filter element for filtering the permeate obtained by filtration with a ceramic microfilter, and wherein the filtration can produce a potassium concentre, wherein said reverse osmosis filter unit (29) is connected to the waste water tank (25, 214, 311, 407). wastewater from the wastewater reservoir (25, 214, 311, 40?) to the reverse osmosis filter unit (29) and wherein the reverse osmosis filter unit (29) to a brain potassium solution reservoir (26, 113). 310) is coupled such that the potassium concentrate from the reverse osmosis filter unit (29) is introduced into the potassium solution collecting vessel (26, 113, 310), and wherein the reverse osmosis filter unit (29) has an outlet through which the reverse osmosis filter the permeate can be withdrawn from the plant where the potassium solution collecting container (28, 113, 310) has an outlet for potassium concentrate through which the potassium bridging can be removed 123. The widow according to claim 82, characterized in that the high pressure lime cooking unit (9, 103, 203, 303, 403) consists of two elongated horizontal tubular chambers having a central conveyor screw, one of the chambers being one to the other. is fixed. 124. The plant according to claim 123, characterized in that the conveying and homogenizing system (8) for conveying the homogenized organic material containing solids and transferring it to the high pressure lime digestion unit (9, 103, 203, 303, 403) and containing an integrated macerator (30), 126. The plant according to claim 124, characterized in that a lime feed ski container (4) is connected to the upper chamber of the high pressure lime cooking unit (9, 103, 203, 303,403), while the high pressure lime cooking unit (9, 103, 203, 303). 403) its lower chamber is connected to a mixing tank (10) connected to a main receiving tank (3) for receiving organic slurry, wherein the mixing tank (10) is conveyed from the main receiving vessel (3) to the mixing tank (10) servants to mix organic slurry. 128. The plant of claim 97, wherein the ammonia absorption unit (21) comprises a two-stage gas condenser condenser in which the ammonia is first reversed by a cooled ammonia condensate »'♦ y» ** * * * X> «Λ - it is condensed in 100 streams and then in a first step in the second condensing step, it is condensed in an upstream stream of water in a non-condensed stream of water. 127. The mill of claim 128, wherein in the second step sulfuric acid is admixed to the countercurrent water. 128. The widow of claim 127, wherein the final ammonia condensate contains ammonia in a concentration greater than 25% by volume. 128. The plant of claim 119, wherein the anaerobic pretreatment digester (115, 213) is a thermophilic digester. 130. The plant of claim 119, wherein the anaerobic pretreatment digester (115,213) is a mesophilic digester. 131. The widow of claim 32, wherein the biogas comprises predominantly methane. 132. The plant of claim 121, wherein the reverse osmosis unit (29) containing the ceramic microfilter filters particles larger than 0.1 µm from the water. 133. The plant of claim 121, wherein the potassiumoneeotrate is produced from the waste water by using a gas engine (28) for heating the spent water used to heat the dextral centrifugation step, wherein the heating results in a distillate containing potassium concentrate, 134. The plant of claim 121, wherein the permeate is used to rinse manure passages in the barn or barn (1, 101, 201, 301, 401), 135. A spin according to claim 82, wherein the organic material comprises at least one of: corn, energy crops, sugar beet, vegetable residues. · * ♦ -101 136. Plant according to claim 82, characterized in that the organic material contains carcasses or parts thereof. 137. The plant of claim 82, wherein the organic material comprises slaughterhouse waste, 138. The widow of claim 82, wherein the organic material comprises a bony stump. 139. The plant of claim 82, wherein the organic material comprises blood plasma, 140. The plant of claim 82, wherein the organic material comprises a substance that is hazardous and non-hazardous in terms of the potential presence of 8SE-prions or other prions. 141. The widow according to claim 62, wherein the organic material comprises animal material having a nitrogen content of greater than 10% by volume. 142. The plant of claim 82. characterized in that the organic material contains more than 10 volumes of cellulose and / or hemicelluloses and / or complex lignin-containing carbohydrates, 143. The plant of claim 82, wherein the organic material comprises more than 50% v / v of cellulose and / or hemicellulose and / or lignin. 144. A ^ 2. Plant according to claim 1, characterized in that the organic material contains organic manure and slurry formed therefrom. 145. The plant of claim 144, wherein the organic manure is cattle manure, pig manure or poultry manure. * í * * χ Φ *** The plant of claim 82, wherein the organic material comprises a deep litter. 147. The plant of claim 82. characterized in that the organic material contains silage. 148. The plant of claim 82, wherein the organic material comprises sugar beet, corn and alfalfa. 149. A 82-148. Use of a plant according to any one of claims 1 to 10 for reducing or eliminating the discharge into the environment of litigation, organisms, ammonia, contaminated air or liquid from pens or stables (1,101, 201, 301, 401). 150. A 82-148. Use of a plant according to any one of claims 1 to 6 for increasing the use of energy-containing organic matter. 181. A 82-148. Use of a plant according to any one of claims 1 to 6 for increasing the production of biogas containing methane gas. 152. A 82-148. Use of a plant according to any one of claims 1 to 4 for separating the nitrogen, phosphorus and potassium fractions from organic materials, wherein said fractions are suitable for use as fertilizers. , 4 ^: <. zx